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
  • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
  • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
  • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
  • C10G65/08—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a hydrogenation of the aromatic hydrocarbons
• • 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
  • C10G2400/20—C2-C4 olefins

Definitions

• the invention relates to a process for the production of low molecular weight olefins from heavy hydrocarbons with a hydrogenating pretreatment and a subsequent thermal cleavage of at least part of the hydrogenation product.
• Light feedstocks are required for the splitting of hydrocarbons for the production of olefins, i.e. Hydrocarbons with a boiling point below 200 ° C, for example naphtha, are particularly suitable. They lead to high splitting yields and result in few undesirable by-products.
• the invention has for its object to design a method of the type mentioned in such a way that it can be operated under particularly favorable economic conditions and in which the conversion in the low-polyaromatic hydrocarbon fraction is also as low as possible.
• This object is achieved in that the hydrogenation is carried out in two stages, the polyaromatic content of a first, polyaromatic-rich hydrocarbon fraction being selectively degraded in the first stage, and the hydrocarbons being refined in the second stage, and a second stage in addition heavy, low-aromatic hydrocarbon fraction is fed ..
• the procedure according to the invention leads to high olefin yields which are equivalent to those of naphtha.
• the partially joint processing of a polyaromatic rich and a low polyaromatic hydrocarbon fraction results in significantly better product qualities in the hydrogenated fractions.
• the quality of the product portion achieved with a boiling point higher than 340 ° C corresponds to products in conventional processes for which considerably higher hydrogenation pressures are required.
• the invention is based on the knowledge that the refining on at least partially split (cracked) molecules takes place considerably better than on uncracked molecules (polyaromatics). It is believed that this is due to the fact that in the hydrogenation of the polyaromatic-rich hydrocarbon fraction, essentially only the polyaromatic compounds are hydrogenated and cracked (selective degradation), but not the monoaromatic compounds. Thus, in the second hydrogenation stage, the double bonds are hydrated and, at the same time, further desulphurization of the insert takes place under conditions which are considerably easier than in conventional processes. As a result of the dilution of the hydrogenated product fraction from the first stage by a fraction low in polyaromatics, the thermodynamic equilibrium is also favorably influenced.
• the space velocity in the first stage is advantageously 0.5 to 4 h -1 , preferably 1 to 2 h -1 , and in the second stage 1 to 6 h, preferably 2 to 4 h
• vacuum gas oil is used as the polyaromatic-rich hydrocarbon fraction and atmospheric gas oil as the polyaromatic-poor hydrocarbon fraction.
• vacuum gas oil (VGO) was used as the polyaromatic-rich hydrocarbon fraction and atmospheric gas oil (AGO) with the properties according to Table 1 as the low-polyaromatic hydrocarbon fraction.
• Table 4 lists the product yields of the first and second stage in the inventive common GO AGO + V H ydrie- tion are combined and the product distributions for the separate AGO VGO and workup.
• the yields of product fractions are given in% by weight based on the use.
• the two-stage joint hydrogenation of AGO and VGO shows very great advantages with regard to the achievable degradation rates compared to the single-stage, separate mode of operation.
• 99.36% sulfur compounds, 99.8% N-base degradation, 86.18% polyaromatic and 88.2% bromine number degradation are achieved in two stages in the VGO cut. These values are excellent for a 100 bar hydrogenation and far exceed the values of the single-stage, separate hydrogenation treatment.
• the differences that can be achieved at AGO are smaller, since the refining of this cut is much easier.
• the process according to the invention achieves a hydrogenation yield at 100 bar, which corresponds to a hydrogenation product which is achieved at a pressure which is higher than 50 bar.

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)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Catalysts (AREA)

Priority Applications (1)

Applications Claiming Priority (2)

Publications (3)

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ID=6172161

Family Applications (1)

Country Status (5)

Cited By (3)

Families Citing this family (10)

Family Cites Families (8)

• 1982
  • 1982-08-31 DE DE19823232395 patent/DE3232395A1/de not_active Withdrawn
• 1983
  • 1983-08-26 DE DE8383108396T patent/DE3361350D1/de not_active Expired
  • 1983-08-26 EP EP83108396A patent/EP0102594B1/fr not_active Expired
  • 1983-08-26 AT AT83108396T patent/ATE16713T1/de not_active IP Right Cessation
  • 1983-08-29 JP JP58156566A patent/JPS5959788A/ja active Pending
• 1984
  • 1984-12-19 US US06/683,764 patent/US4619757A/en not_active Expired - Fee Related

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