CN116410787A - Method for producing light weight reforming material and ethylene cracking raw material by diesel oil hydrotreating selective recycle - Google Patents
Method for producing light weight reforming material and ethylene cracking raw material by diesel oil hydrotreating selective recycle Download PDFInfo
- Publication number
- CN116410787A CN116410787A CN202111643539.5A CN202111643539A CN116410787A CN 116410787 A CN116410787 A CN 116410787A CN 202111643539 A CN202111643539 A CN 202111643539A CN 116410787 A CN116410787 A CN 116410787A
- Authority
- CN
- China
- Prior art keywords
- raw material
- diesel
- distillation section
- distillation
- hydrocracking
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000002994 raw material Substances 0.000 title claims abstract description 55
- 238000005336 cracking Methods 0.000 title claims abstract description 48
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 35
- 239000005977 Ethylene Substances 0.000 title claims abstract description 35
- 239000002283 diesel fuel Substances 0.000 title claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- 239000000463 material Substances 0.000 title claims abstract description 16
- 238000002407 reforming Methods 0.000 title abstract description 13
- 238000004821 distillation Methods 0.000 claims abstract description 61
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 53
- 238000006243 chemical reaction Methods 0.000 claims abstract description 36
- 238000000034 method Methods 0.000 claims abstract description 20
- 238000004064 recycling Methods 0.000 claims abstract description 16
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 10
- 239000001257 hydrogen Substances 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 6
- 238000002156 mixing Methods 0.000 claims abstract description 4
- 239000000203 mixture Substances 0.000 claims abstract description 4
- 238000000926 separation method Methods 0.000 claims abstract description 4
- 238000005194 fractionation Methods 0.000 claims abstract description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 7
- 150000002431 hydrogen Chemical class 0.000 claims description 2
- 238000012958 reprocessing Methods 0.000 claims 2
- 239000012188 paraffin wax Substances 0.000 abstract description 19
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 6
- 150000005671 trienes Chemical class 0.000 abstract description 3
- 125000000753 cycloalkyl group Chemical group 0.000 abstract description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 238000007670 refining Methods 0.000 description 25
- 125000003118 aryl group Chemical group 0.000 description 11
- 239000003054 catalyst Substances 0.000 description 8
- 239000003502 gasoline Substances 0.000 description 8
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical group C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000001993 wax Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000001833 catalytic reforming Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007142 ring opening reaction Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000003350 kerosene Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000005504 petroleum refining Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000004148 unit process Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
-
- 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
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a method for producing a light weight reforming material and an ethylene cracking raw material by diesel oil hydrotreating and selective recycling, which comprises the following steps: (a) Mixing the diesel raw material with hydrogen, and carrying out hydrofining and hydrocracking; (b) After gas-liquid separation, steam stripping and fractionation are carried out on the hydrogenation mixture flow obtained in the step (a), a first distillation section, a second distillation section and a third distillation section are respectively obtained, the final distillation point of the first distillation section is no more than 140 ℃, the final distillation point of the second distillation section is no more than 250 ℃, and the bottom oil of the fractionating tower is the third distillation section; (c) And (3) completely recycling the generated second fraction to the hydrofining or hydrocracking reaction unit for recycling. The method maintains the paraffin content in unconverted oil and ethylene cracking raw material to the maximum extent, improves the triene yield of the ethylene cracking raw material, further improves the yield of light naphtha, and simultaneously transfers heavy aromatic hydrocarbon and heavy cyclic hydrocarbon into light fraction, and improves the yield of the reforming material.
Description
Technical Field
The invention belongs to the field of petroleum refining, and relates to a method for producing a light weight reforming material and an ethylene cracking raw material by selective recycling of diesel oil hydrotreating.
Background
With the gradual improvement of the oil refining capability of China, the relatively low cost of the whole economy and the gradual improvement of new energy and sustainable development energy in the whole energy structure, the requirements of China on traditional gasoline and diesel clean fuels are gradually slowed down, and particularly the requirements of diesel are increased negatively. Taking the structure of the refinery product as an example, the yield of the light oil product is 50-60%, and the enterprises integrating the refining and the integration can approach 35-40%. The high yield characteristic of the light oil product promotes the current enterprises to carry out the secondary conversion of gasoline, diesel oil and aviation kerosene. At present, the demands of chemical raw materials are vigorous, wherein the increase of ethylene and propylene is rapid, and meanwhile, the demands of chemical raw materials such as BTX and the like are also very vigorous. Therefore, the technology for maximizing the yield of ethylene material and producing other reforming raw materials such as naphtha is particularly important.
As national VII gasoline of genie VII or higher may require forward gasoline dry point, refineries need to make naphtha lighter or reform feedstock lighter.
From the standpoint of the steam-cracked feedstock, suitable steam-cracked feedstocks include conventional straight run naphtha, light naphtha, ethane, hydrocracked tail oil, and the like. The main routes for ethylene production are therefore: (1) The technical route for producing chemical raw materials by wax oil hydrocracking can ensure that the oriented conversion of vacuum wax oil fraction can produce high-quality raw materials suitable for ethylene cracking by introducing a catalyst with suitable activity and selective ring opening, and has a BMCI value of no more than 12 and high paraffin content. (2) The technological route of diesel oil solvent extraction dearomatization reduces naphthenes and most aromatic hydrocarbons in straight-run diesel oil through the effect of polar separation, improves the paraffin content in raffinate oil, and realizes the substantial reduction of diesel oil BMCI value. (3) The diesel hydrocracking process realizes aromatic saturation and naphthene ring opening in diesel, and ensures that low BMCI value components are largely reserved, but diesel hydrocracking and wax oil hydrocracking are slower in reaction rate than wax oil hydrocracking reaction rate due to the difference of raw materials and the difference of reaction processes, and a large amount of gas components are easily generated in diesel hydrocracking.
Liu Jianwei et al (petroleum refining and chemical industry, 2020, 51 (9): 34-40) report that when straight-run diesel is processed by a conventional hydrocracking process with a single-stage dual-agent tandem hydrocracking, the BMCI value of the unconverted oil fraction > 180 ℃ is reduced to 18.8 under the condition of controlling the naphtha yield to 10%, but the diesel fraction still contains a large amount of naphthenes (30-40 wt%) and the relative paraffin content is increased by 5-8 percentage points. Although capable of meeting ethylene feed requirements, such high BMCI triene yields still have a gap from other readily cleavable components.
CN1955261a discloses a poor quality catalytic cracking diesel hydrocracking method. The method mixes poor quality catalytic diesel with heavy hydrocracking raw materials, carries out hydrocracking first, and carries out secondary hydrocracking on the obtained middle distillate oil to obtain high aromatic heavy naphtha and tail oil with low BMCI value. The middle distillate oil obtained in one step has no sulfur, nitrogen and other impurities, and the catalyst activity is fully utilized, so that the catalyst can be operated at a higher space velocity and a lower temperature, and even at a lower hydrogen partial pressure, and the economy is improved. And the lower hydrogen partial pressure is beneficial to converting middle distillate into heavy naphtha with high aromatic potential, and the lower temperature reduces the further cracking of the heavy naphtha, thereby greatly improving the yield of the heavy naphtha. The process is mainly described for catalytic cracking diesel conversion and middle distillate processing, but is not reported for how to produce naphtha and ethylene for straight-run diesel hydroconversion, nor is it described how to maximize the production of naphtha for straight-run diesel.
CN102453535a discloses a hydrocracking method for increasing the yield of the reforming material, the raw oil and hydrogen are mixed and then sequentially subjected to a hydrofining reaction and a hydrocracking reaction, the reaction effluent is cooled and separated, and the obtained light diesel oil fraction with the temperature of 10% -100% and 220 ℃ -320 ℃ is returned to the hydrocracking reactor for continuous reaction. Because the content of aromatic hydrocarbon and naphthene in the fraction is high, the fraction is a suitable fraction for increasing yield of high-quality heavy naphtha; the recovery of the above fractions also increases the aviation kerosene yield and increases the cetane number of the diesel fraction. By adopting the method provided by the invention, the recycled light diesel fraction enters the hydrocracking reactor instead of the raw material tank, and does not pass through the hydrofining reactor, so that the aromatic hydrocarbon and naphthene part of the light diesel fraction is less subjected to hydrogenation saturation reaction, thereby being beneficial to improving the aromatic potential of heavy naphtha and reducing hydrogen consumption. Although this method discloses a naphtha yield increase, it does not allow for ethylene production.
Because the raw materials in the hydrocracking reaction process of the diesel are mainly concentrated in the range of 180-350 ℃, the carbon number molecules are smaller, the current diesel hydrogenation conversion pressure level is low, the conversion of most aromatic hydrocarbon and naphthene cannot be realized, and the matched process and catalyst are required to cooperate to realize the production of the ethylene cracking raw material with low BMCI value by the mixed diesel. Meanwhile, in the hydrocracking conversion process of diesel oil, unconverted oil is generated, the BMCI value is gradually reduced along with the increase of the boiling point, the paraffin content of the fraction at 180-250 ℃ is relatively low, about 10-40 wt%, and the fraction is not a high-quality ethylene cracking raw material, and also the reformed raw material cannot be used as qualified reformed raw material at 180-200 ℃ in consideration of the reformed raw material, because the dry point of the gasoline fraction can be obviously improved after catalytic reforming. Considering the condition that the standard dry point of future gasoline is advanced compared with the existing standard dry point of gasoline, the dry point of the feed for catalytic reforming also needs to be advanced. Considering the specificity of 180-250 ℃ fraction and heavy naphtha (140-180 ℃ fraction) and the fact that the catalyst is not suitable for being used as an ethylene cracking raw material and a heavy reforming raw material, the catalyst is light based on the characteristic that the content of cycloparaffin molecules and heterogeneous cycloparaffin molecules is relatively high, and the catalyst can effectively solve the problem of outlet.
Disclosure of Invention
Aiming at the development trends that BMCI values in the diesel hydrocracking unconverted diesel are unevenly distributed along with the distillation range, the BMCI value of the diesel is limited to be improved under the condition of lower conversion rate, and the paraffin content in the hydrocracking unconverted diesel is relatively low and the future gasoline dry point is advanced, in order to further improve the utilization efficiency of the straight-run diesel, the invention provides a process route for selectively recycling the diesel hydrotreating to produce high-quality ethylene materials and light-weight reformed raw materials.
In order to achieve the above object, the present invention provides a method for producing a light weight reforming material and an ethylene cracking raw material by selective recycling of diesel oil hydrotreating, comprising the steps of:
(a) Mixing the diesel raw material with hydrogen, and carrying out hydrofining and hydrocracking;
(b) After gas-liquid separation, steam stripping and fractionation are carried out on the hydrogenation mixture flow obtained in the step (a), a first distillation section, a second distillation section and a third distillation section are respectively obtained, the final distillation point of the first distillation section is no more than 140 ℃, the final distillation point of the second distillation section is no more than 250 ℃, the bottom oil of the fractionating tower is the third distillation section, the first distillation section can be used as a reforming raw material, and the third distillation section can be used as an ethylene cracking raw material;
(c) And (3) completely recycling the generated second fraction to the hydrofining or hydrocracking reaction unit for recycling.
The material flow and the product obtained by the whole reaction process flow are a first distillation section and a third distillation section. The relative enrichment of the paraffin, the naphthene and the aromatic hydrocarbon can be realized by effectively regulating and controlling the initial distillation point and the final distillation point of the fraction through the fractionating tower, the higher 60-80wt% of the paraffin in the third fraction section is realized, and the light naphtha yield is improved.
The invention relates to a method for producing light weight heavy material and ethylene raw material by diesel oil hydrotreating and selective recycling, wherein the diesel oil raw material is straight-run diesel oil and/or coked diesel oil.
The invention relates to a method for producing light weight reforming material and ethylene cracking raw material by diesel oil hydrotreating selective remixing, which comprises the following steps: the reaction pressure is 6-15Mpa, preferably 6-10Mpa, the reaction temperature is 330-380 ℃, preferably 350-370 ℃; hydrocracking process conditions: the reaction pressure is 6-15Mpa, preferably 6-10Mpa, the reaction temperature is 345-390 ℃, preferably 345-370 ℃, and the reaction space velocity of hydrofining and hydrocracking is 0.5-3.0h -1 The hydrogen oil volume ratio is 500-1500 v/v, preferably 500-1000v/v.
The invention relates to a method for producing light weight reforming material and ethylene cracking raw material by diesel oil hydrotreating selective recycle, wherein a first distillation section can be divided into two sub-distillation sections, the final distillation point is no more than 90 ℃, the final distillation point is no more than 140 ℃ in the first distillation section 1A and the first distillation section 1B. Wherein the first distillation section 1A can be used as an ethylene cracking raw material, and the first distillation section 1B can be used as a catalytic reforming raw material.
In the method for producing the light weight reforming material and the ethylene cracking raw material by selective recycling of diesel oil hydrotreating, in the step (c), the second fraction can be recycled to the feed of a hydrofining reactor or to the feed of a second hydrocracking reactor, and the mass ratio of the hydrofining feed or the hydrocracking feed to the recycled second fraction is 1:1-10:1, preferably 3:1-10:1.
The second distillation range is 140-250deg.C, and can be adjusted to 140-250deg.C, 180-250deg.C, 140-235 deg.C or 140-250deg.C according to the regulation of target product.
The invention has the beneficial effects that:
according to the invention, the structure of a target product and the molecular structure in the reaction unit process are optimally regulated, so that the optimal design of the molecular composition of the target product is realized, on the basis of the primary pass/partial cycle/full cycle process of the traditional diesel hydrocracking, on the basis of the recognition of the molecular structure difference of the diesel hydrocracking product, the directional conversion ring opening of naphthenes is realized by selectively recycling the second fraction section rich in naphthenes to the hydrocracking/hydrofining reaction unit, the paraffins in naphtha are transferred to the light naphtha fraction, the problems of poor paraffin conversion selectivity and the like caused by recycling the traditional heavy unconverted oil are avoided, the paraffin content in the unconverted oil and ethylene cracking raw material is reserved to the maximum extent, the triene yield of the ethylene cracking raw material is improved, the yield of the light naphtha is further improved, and the heavy aromatics and heavy cyclic hydrocarbons are transferred to the light fraction, so that the yield of the heavy monolith is improved.
Drawings
FIG. 1 is a process flow diagram of the selective recycle of diesel hydrotreatment to produce a light reformate and an ethylene cracking feedstock in accordance with the present invention.
Wherein, the reference numerals:
1, a diesel raw material; 2 hydrogen; 3, a hydrofining reactor; 4 hydrofining stream; 5a hydrocracking reactor; 6 hydrocracking the stream; 7, a gas-liquid separator; 8 a liquid stream; 9, a fractionating tower; 10 dry gas and liquefied gas streams; 11 a first distillation section; 12 a second distillation section; 13 a third distillation stage; 14 recycle stream.
Detailed Description
The present invention will be specifically described below by way of examples. It is noted herein that the following examples are given solely for the purpose of illustration and are not to be construed as limiting the scope of the invention, as many insubstantial modifications and variations of the invention will become apparent to those skilled in the art in light of the above disclosure.
As shown in fig. 1, a mixed stream obtained by mixing a diesel raw material 1 and hydrogen 2 enters a hydrofining reactor 3, a hydrofining stream 4 passing through an outlet of the hydrofining reactor 3 enters a hydrocracking reactor 5, a hydrocracking stream 6 flowing out of the outlet of the hydrocracking reactor enters a gas-liquid separator 7, a liquid stream 8 flowing out of an outlet at the bottom of the gas-liquid separator 7 enters a fractionating tower 9, and a hydrocracking product is obtained by passing through the fractionating tower 9, namely a dry gas stream 10 and a liquefied gas stream 10, a first distillation section 11, a second distillation section 12, a third distillation section 13 and the second distillation section 12 as a recycle stream 14 returns to the inlet 4 of the refining reactor or the inlet 5 of the cracking reactor.
Example 1
Straight-run diesel A was used as a raw material, and the properties of the raw material are shown in Table 1. The reaction pressure is 8Mpa through a hydrofining and hydrocracking reactor, and the refining and cracking airspeeds are respectively 2.0h based on fresh feed -1 The hydrogen-oil ratio is 800, the refining temperature is 350 ℃, the cracking temperature is 345 ℃, the second fraction is totally recycled to the refining reactor, the distillation range is 140-250 ℃, the fresh feed proportion is about 25wt%, the BMCI value of the obtained third fraction is 12, the paraffin content is 65.2wt%, the yield is 58%, the light naphtha yield is 5wt% (IBP-65 ℃), and the aromatic potential of the light heavy naphtha (65-140 ℃) is 45%.
Example 2
The straight-run diesel A is used as raw material, and is passed through hydrofining and hydrocracking unit reactor, pressure is 10Mpa, and refining and cracking airspeed are respectively 1.8h -1 The hydrogen-oil ratio is 1000, the refining temperature is 338 ℃, the cracking temperature is 358 ℃, the second fraction is totally recycled to the inlet of the refining reactor, the distillation range is 140-250 ℃, the fresh feed proportion is about 20wt%, the yield of the third fraction (250-FBP) is about 58wt%, the BMCI value is about 12.4, the paraffin content is 63wt%, the IBP-65 ℃ of the light naphtha fraction is about 4.0wt%, the aromatic potential is 44% of the light heavy naphtha fraction is 65-140 ℃.
Comparative example 1
The straight-run diesel A is used as raw material, and is passed through hydrofining and hydrocracking reactor, its pressure is 8Mpa, and its refining and cracking airspeed are respectively 2.0h -1 The hydrogen-oil ratio is 800, the refining temperature is 350 ℃, the cracking temperature is 345 ℃, the yield of the third fraction (180-FBP) is about 58.2wt%, the BMCI value is about 13.98, the paraffin content is 61.6wt%, the heavy naphtha distillation range is 65-180 ℃, and the aromatic potential is 40wt%.
Comparative example 2
Straight-run diesel oil A is used as raw material, through the processes ofThe pressure of the reactor is 8Mpa, and the space velocity of refining and cracking is 2.0h respectively based on fresh feed -1 The hydrogen-oil ratio is 800, the refining temperature is 350 ℃, the cracking temperature is 345 ℃, and the catalyst is prepared>The distillate oil of 30wt% in the distillate oil at 180 ℃ is recycled to the inlet of the refining reactor, the recycling amount accounts for 20wt% of the fresh feed, the paraffin content of the obtained third distillation section (180-FBP) is about 60wt%, and the yield of the hydrocracking unconverted oil is 45wt%.
Comparative example 3
The straight-run diesel A is taken as raw material, and is subjected to a hydrofining and hydrocracking reactor with the pressure of 8Mpa, and the refining and cracking airspeed is respectively 2.0h based on fresh feed -1 The hydrogen-oil ratio is 800, the refining temperature is 350 ℃, the cracking temperature is 345 ℃,>the 180℃fraction was completely recycled to the inlet of the refining reactor, and was thrown outward by 0.5wt%, the paraffin content of the unconverted oil was 85wt%, the BMCI value was 6.2, and the yield was 0.5wt%. The yield of heavy naphtha is 75wt% (65-180 ℃), the aromatic potential of heavy naphtha is 40wt%, and the yield of light naphtha is 25wt% (IBP-65 ℃).
Example 3
The straight-run diesel A is taken as raw material, and is subjected to a hydrofining and hydrocracking reactor, the reaction pressure is 8Mpa, and the refining and cracking airspeed is 2.0h respectively based on fresh feed -1 The hydrogen-oil ratio is 800, the refining temperature is 348 ℃, the cracking temperature is 345 ℃, the second fraction range is 140-250 ℃, the second fraction is totally recycled to the cracking reactor, the recycled fraction accounts for about 25wt% of the fresh feed, the BMCI value of the obtained hydrocracking unconverted oil fraction is 12.2, the paraffin content is 65wt%, and the light naphtha (IBP-65 ℃) yield is 4.8wt%.
Example 4
The straight-run diesel oil B is used as raw material, and is passed through hydrofining and hydrocracking reactor, its pressure is 8Mpa, hydrogen-oil ratio is 600, and the refining and cracking airspeed is 1.5 hr respectively -1 The refining temperature is 362 ℃ and the cracking temperature is 363 ℃, wherein the second fraction is recycled to the inlet of the cracking reactor in a stage of 100-250 ℃ and accounts for about 20wt% of fresh feed, the third fraction yield (250-FBP) is about 82wt%, the BMCI value is about 11.5, the paraffin content is 62.3wt%, and the light naphtha (IBP)-65 ℃ to yield 4.0wt%, the sum of the ethylene cracking feed is 86.0wt%, the naphtha yield 13wt%, and the aromatic potential 42wt%.
Comparative example 4
The straight-run diesel oil B is used as raw material, and is passed through hydrofining and hydrocracking reactor, its pressure is 8Mpa, hydrogen-oil ratio is 600, and the refining and cracking airspeed is 1.5 hr respectively -1 Refining temperature is 362 ℃, cracking temperature is 363 ℃,>the fraction yield at 180℃was about 85wt%,>the BMCI value of the 180 ℃ fraction is about 14.58, the paraffin content is 59.7wt%, the yield of naphtha (IBP-180 ℃) is 13wt% and the aromatic potential is 39wt%.
Example 5
Straight-run diesel oil B+10% coked diesel oil is used as raw material, and is passed through hydrofining and hydrocracking reactor, its pressure is 8Mpa, hydrogen-oil ratio is 600, and the refining and cracking airspeed is 1.5 hr respectively -1 The refining temperature is 362 ℃ and the cracking temperature is 365 ℃, wherein the second distillation stage is recycled to the inlet of the cracking reactor, the distillation range is 100-250 ℃, the fresh feed proportion is about 20wt%, the third distillation yield is about 82wt%, the BMCI value of the third distillation stage is about 11.5, the paraffin content is 62.3wt%, the light naphtha (IBP-65 ℃) yield is 4.0wt%, the sum of the light naphtha (IBP-65 ℃) and the ethylene cracking raw materials is 86.0wt%, the naphtha (65-100 ℃) yield is 13wt%, and the aromatic potential is 42wt%.
TABLE 1 basic Properties of straight run Diesel
The invention can realize the high-efficiency utilization of molecules through the selective recycling process of the hydrocracking product, and recycle the hydrogenation product with a cycloparaffin-rich structure to produce light naphtha while increasing the yield of high-quality ethylene cracking raw materials, thereby reducing the dry point of the naphtha and optimizing the quality of ethylene products.
Of course, the present invention is capable of other various embodiments and its several details are capable of modification and variation in light of the present invention by one skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (5)
1. A method for producing a light weight reformate and an ethylene cracking feedstock by selective recycle of diesel hydrotreating, comprising the steps of:
(a) Mixing the diesel raw material with hydrogen, and carrying out hydrofining and hydrocracking;
(b) After gas-liquid separation, steam stripping and fractionation are carried out on the hydrogenation mixture flow obtained in the step (a), a first distillation section, a second distillation section and a third distillation section are respectively obtained, the final distillation point of the first distillation section is no more than 140 ℃, the final distillation point of the second distillation section is no more than 250 ℃, and the bottom oil of the fractionating tower is the third distillation section;
(c) And (3) completely recycling the generated second fraction to the hydrofining or hydrocracking reaction unit for recycling.
2. The method for producing light weight heavy material and ethylene raw material by diesel oil hydrotreating and selective recycle according to claim 1, wherein the diesel oil raw material is straight-run diesel oil and/or coker diesel oil.
3. The method for producing light weight reformate and ethylene cracking feedstock by selective recycle of diesel hydrotreating according to claim 1, wherein the process conditions of hydrofining are: the reaction pressure is 6-15Mpa, preferably 6-10Mpa, the reaction temperature is 330-380 ℃, preferably 350-370 ℃; hydrocracking process conditions: the reaction pressure is 6-15Mpa, preferably 6-10Mpa, the reaction temperature is 345-390 ℃, preferably 345-370 ℃, and the reaction space velocity of hydrofining and hydrocracking is 0.5-3.0h -1 The hydrogen oil volume ratio is 500-1500 v/v, preferably 500-1000v/v.
4. The method for producing light weight heavy material and ethylene cracking raw material by selective recycle of diesel oil hydrotreating according to claim 1, wherein the first distillation section is divided into two sub-distillation sections, the first distillation section 1A, the final distillation point is no more than 90 ℃, the first distillation section 1B, the final distillation point is no more than 140 ℃.
5. The process for the selective reprocessing of diesel fuel according to claim 1, wherein in step (c) the mass ratio of hydrofinishing feed or hydrocracking feed to the second fraction of the reprocessing is from 1:1 to 10:1, preferably from 3:1 to 10:1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111643539.5A CN116410787A (en) | 2021-12-29 | 2021-12-29 | Method for producing light weight reforming material and ethylene cracking raw material by diesel oil hydrotreating selective recycle |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111643539.5A CN116410787A (en) | 2021-12-29 | 2021-12-29 | Method for producing light weight reforming material and ethylene cracking raw material by diesel oil hydrotreating selective recycle |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116410787A true CN116410787A (en) | 2023-07-11 |
Family
ID=87049748
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111643539.5A Pending CN116410787A (en) | 2021-12-29 | 2021-12-29 | Method for producing light weight reforming material and ethylene cracking raw material by diesel oil hydrotreating selective recycle |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116410787A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1903993A (en) * | 2005-07-26 | 2007-01-31 | 中国石油化工股份有限公司 | Hydrogenation cracking method to produce more raw material for making ethylene |
| CN102453535A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Hydrocracking method for reforming material yield increase |
| CN103013559A (en) * | 2011-09-22 | 2013-04-03 | 中国石油化工股份有限公司 | Hydrocracking method for selective increasing of aviation kerosene yield |
-
2021
- 2021-12-29 CN CN202111643539.5A patent/CN116410787A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1903993A (en) * | 2005-07-26 | 2007-01-31 | 中国石油化工股份有限公司 | Hydrogenation cracking method to produce more raw material for making ethylene |
| CN102453535A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Hydrocracking method for reforming material yield increase |
| CN103013559A (en) * | 2011-09-22 | 2013-04-03 | 中国石油化工股份有限公司 | Hydrocracking method for selective increasing of aviation kerosene yield |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103270143B (en) | Process for the refining of crude oil | |
| CN102061195A (en) | Process to produce high quality kerosine and diesel fuels and hydrogen coproduction from light saturated fractions | |
| CN102796559A (en) | Method and apparatus for producing fuel oil by hydrocracking | |
| CN104277879B (en) | A kind of two-stage slurry bed system hydrogenation technique of middle coalite tar | |
| CN113122332B (en) | Production method of low-sulfur marine fuel oil | |
| CN109988645B (en) | Hydrogenation modification and hydrofining combined process for inferior diesel oil | |
| CN109988643B (en) | Hydrogenation modification and hydrofining combined process for poor diesel oil | |
| CN115895722A (en) | System for preparing light aromatic hydrocarbon from heavy oil raw material | |
| CN116410787A (en) | Method for producing light weight reforming material and ethylene cracking raw material by diesel oil hydrotreating selective recycle | |
| CN111484876B (en) | Method for producing aromatic hydrocarbon and high-quality gasoline from poor-quality catalytic cracking diesel oil | |
| CN104178208B (en) | A kind of naphtha is produced the method for high-knock rating gasoline | |
| CN104419461B (en) | The slurry bed system of a kind of coal tar and fixed bed serial hydrogenation technique | |
| CN114437792A (en) | Method and apparatus for processing residual oil | |
| CN105505459A (en) | Catalytic cracking method of heavy oil and device thereof | |
| CN116410781A (en) | Method for producing ethylene raw material by diesel hydrocracking | |
| CN111826197B (en) | Method for producing gasoline from naphtha | |
| CN114437801B (en) | Two-stage hydrocracking method | |
| CN1227336C (en) | Middle pressure hydrocracking and catalytic cracking integrated process | |
| CN115678607B (en) | Heavy crude oil processing method and system for multi-product chemicals | |
| CN115820299B (en) | Method for producing refined naphtha by catalytically cracking gasoline | |
| CN114437783B (en) | Hydrocracking method for producing jet fuel | |
| CN116042270B (en) | Hydrocracking method for producing heavy naphtha and jet fuel | |
| CN111100708B (en) | Hydrocracking method for producing chemical raw materials | |
| CN116042271B (en) | Hydrocracking method for producing heavy naphtha and low-freezing diesel oil | |
| CN109988599B (en) | Flexible hydrogenation modification process for inferior diesel oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |