EP1285903A1 - Verfahren zur Herstellung von Paraffinen aus zyklische Kohlenwasserstoffe enthaltenden Einsatzstoffen - Google Patents
Verfahren zur Herstellung von Paraffinen aus zyklische Kohlenwasserstoffe enthaltenden Einsatzstoffen Download PDFInfo
- Publication number
- EP1285903A1 EP1285903A1 EP02018081A EP02018081A EP1285903A1 EP 1285903 A1 EP1285903 A1 EP 1285903A1 EP 02018081 A EP02018081 A EP 02018081A EP 02018081 A EP02018081 A EP 02018081A EP 1285903 A1 EP1285903 A1 EP 1285903A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- reaction
- reactor
- aromatics
- carried out
- cyclic hydrocarbons
- 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.)
- Granted
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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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
-
- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
Definitions
- the invention relates to a method for producing paraffins from cyclic Feedstocks containing hydrocarbons such as mineral oil fractions and / or Fractions from thermal or catalytic conversion plants containing alkanes, Alkenes, cyclic alkanes and / or aromatics by reaction with a zeolite catalyst.
- hydrocarbons such as mineral oil fractions and / or Fractions from thermal or catalytic conversion plants containing alkanes, Alkenes, cyclic alkanes and / or aromatics
- the present invention has for its object a method of the beginning mentioned type so that high yields in an economical manner can be achieved.
- This object is achieved in that the implementation under Isothermal conditions is carried out in a cooled reactor.
- the conversion of the starting materials into externally cooled Tubes of the reactor performed.
- Heat transfer media are particularly suitable for melts and heat transfer oils.
- the cyclic hydrocarbon feedstocks are advantageously used hydrogenated in a pretreatment stage to a feed stream that predominantly Contains naphthenes and up to 40 vol.% Aromatics.
- a nickel catalyst is expediently used for hydrogenation. From procedural For reasons, it can be advantageous to reduce the aromatic content in the feed stream to below 5 % By volume, preferably at most 2% by volume.
- the cooled reactor is one adiabatic catalyst bed with a hydrogenation catalyst immediately upstream, where by hydrogenation of hydrocarbons resulting waste heat further preheating of the feed materials for the subsequent isothermal reaction is used.
- the use of external energy for Heating of the feed materials to those necessary for the isothermal reaction Reaction temperature can be minimized, and there is no need for an oven.
- the pretreatment stage shown in Figure 1 is used to hydrogenate the cyclic Feedstocks containing hydrocarbons.
- a stream of C5 + Hydrocarbons from an olefin plant undergo selective hydrogenation and Desulfurization and fractionation 1 fed.
- the pyrolysis heavy gasoline obtained with predominantly C7 + hydrocarbons has an aromatic content from typically 60 to 90% by volume, in the present example 87% by volume.
- a pump 2 turns the pyrolysis heavy gasoline to a pressure of approx. 30 bar compressed and divided into two partial streams 3 and 4.
- the partial stream 4 is a Heat exchanger 5 heated and one with a temperature of 80 to 120 ° C.
- Hydrogenation stage 6 with three catalyst beds which contain a nickel catalyst, given up.
- the other partial stream 3 is distributed to the hydrogenation stage 6.
- the aromatics are hydrogenated to naphthenes.
- the product obtained which can contain up to 40 vol.% aromatics, but smaller in the present example 0.5 vol.% Aromatics, is at a temperature of 120 to 160 ° C by means of Line 7 withdrawn, cooled in the heat exchangers 5 and 8, the Heat exchanger 8 is operated with cooling water, and finally one Gas-liquid separation 9 supplied. Liquid product is partly via line 10 recycled and serves to dilute the feedstock for hydrogenation stage 6.
- the resulting hydrogen gas is in a pressure swing adsorption system (PSA) 11 hydrogen produced were added.
- PSA pressure swing adsorption system
- the product stream containing the naphthenes is by means of a Pump 13 to about 25 to 70 bar, preferably 50 to 60 bar, in the present example compressed about 60 bar, preheated by means of heat exchangers 14 and 15 and one Heating level 16 supplied.
- the feed materials heated to approx. 380 ° C are used in the Isothermal reactor 17 initiated.
- the Isothermal reactor 17 designed as a straight tube reactor.
- the arranged in the reactor 17 Pipes are cooled from the outside with a heat transfer oil, which is in line 18 circulated.
- the heat of reaction occurring in the reactor 17 is by means of Heat transfer oil discharged to an external steam generator 19.
- the isothermal reactor 17 contains a zeolite catalyst.
- the naphthenes are placed in the reactor isothermal conditions with a constant high conversion rate to paraffins implemented.
- the reaction products are discharged via line 20 and by means of Heat exchangers 15 and 14 cooled. At one above the dew point Temperature of 144 ° C, the reaction products to that shown in Figure 3 Submit post processing level.
- the reaction products fractionated.
- the reaction products are passed to a scrubber 22 via line 21 fed.
- the gaseous product is discharged from the head of the scrubber 22 via line 23 dissipated, cooled in a heat exchanger 24 against cooling water and a gas-liquid separation 25 fed.
- the gaseous product obtained is about Line 26 fed to a further gas-liquid separation stage 27. That in this Separation stage resulting gaseous product is at a temperature of approx. 15 ° C passed through a dryer 28 to a plate heat exchanger 29.
- gaseous hydrogen is separated and by means of Line 31 fed into the process.
- the liquid obtained in the separation stage 30 The product is finally discharged from the aftertreatment stage via line 32 and stands as a feed with a very high paraffin content for the steam cracker Olefin plant available.
- the condensate obtained in the scrubber 22 contains partially propane, and is via line 33 of a propane stripping in a Stripping column 34 fed. Aromatics that are produced in the process are finally added a return line 35 to the pretreatment stage shown in FIG. 1 recycled.
- FIG. 4 shows the product composition of the product leaving the plant Product stream specified as the insert for the steam cracker of the olefin plant is used (SC feedstock).
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Crystallography & Structural Chemistry (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
Description
- Figur 1
- ein Fließschema der Vorbehandlungsstufe
- Figur 2
- ein Fließschema der isothermen katalytischen Umsetzung
- Figur 3
- ein Fließschema der Nachbearbeitungsstufe.
- Figur 4
- eine Auflistung der Produktbestandteile
Claims (6)
- Verfahren zur Herstellung von Paraffinen aus zyklische Kohlenwasserstoffe enthaltenden Einsatzstoffen wie Mineralölfraktionen und/oder Fraktionen aus thermischen oder katalytischen Konversionsanlagen enthaltend Alkane, Alkene, zyklische Alkane und/oder Aromaten durch Umsetzen mit einem Zeolith-Katalysator, dadurch gekennzeichnet, dass die Umsetzung unter isothermen Bedingungen in einem gekühlten Reaktor durchgeführt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Umsetzung in von außen gekühlten Rohren des Reaktors durchgeführt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Umsetzung in einem Reaktor mit gewickelten Rohren durchgeführt wird.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass die die zyklischen Kohlenwasserstoffe enthaltenden Einsatzstoffe in einer Vorbehandlungsstufe zu einem Einsatzstrom hydriert werden, der überwiegend Naphthene und bis zu 40 Vol.% Aromaten enthält.
- Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass der Einsatzstrom weniger als 5 % Aromaten enthält.
- Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass dem gekühlten Reaktor ein adiabates Katalysatorbett mit einem Hydrierkatalysator unmittelbar vorgeschaltet ist, wobei durch Hydrierung von Kohlenwasserstoffen anfallende Reaktionswärme zur Vorheizung der Einsatzstoffe für die anschließende Isothermreaktion eingesetzt wird.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10139726A DE10139726A1 (de) | 2001-08-13 | 2001-08-13 | Verfahren zur Herstellung von Paraffinen aus zyklische Kohlenwasserstoffe enthaltenden Einsatzstoffen |
DE10139726 | 2001-08-13 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1285903A1 true EP1285903A1 (de) | 2003-02-26 |
EP1285903B1 EP1285903B1 (de) | 2006-03-22 |
Family
ID=7695305
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP02018081A Expired - Lifetime EP1285903B1 (de) | 2001-08-13 | 2002-08-13 | Verfahren zur Herstellung von Paraffinen aus zyklische Kohlenwasserstoffe enthaltenden Einsatzstoffen |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP1285903B1 (de) |
AT (1) | ATE321014T1 (de) |
DE (2) | DE10139726A1 (de) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10563130B2 (en) | 2014-07-17 | 2020-02-18 | Sabic Global Technologies B.V. | Upgrading hydrogen deficient streams using hydrogen donor streams in a hydropyrolysis process |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1993008145A1 (en) * | 1991-10-25 | 1993-04-29 | Mobil Oil Corporation | Combined paraffin isomerization/ring opening process |
WO2001027223A1 (de) * | 1999-10-13 | 2001-04-19 | Veba Oil Refining & Petrochemicals Gmbh | Verfahren zur herstellung von n-alkanen aus mineralölfraktionen und katalysator zur durchführung des verfahrens |
-
2001
- 2001-08-13 DE DE10139726A patent/DE10139726A1/de not_active Withdrawn
-
2002
- 2002-08-13 EP EP02018081A patent/EP1285903B1/de not_active Expired - Lifetime
- 2002-08-13 AT AT02018081T patent/ATE321014T1/de not_active IP Right Cessation
- 2002-08-13 DE DE50206118T patent/DE50206118D1/de not_active Expired - Fee Related
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1993008145A1 (en) * | 1991-10-25 | 1993-04-29 | Mobil Oil Corporation | Combined paraffin isomerization/ring opening process |
WO2001027223A1 (de) * | 1999-10-13 | 2001-04-19 | Veba Oil Refining & Petrochemicals Gmbh | Verfahren zur herstellung von n-alkanen aus mineralölfraktionen und katalysator zur durchführung des verfahrens |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10563130B2 (en) | 2014-07-17 | 2020-02-18 | Sabic Global Technologies B.V. | Upgrading hydrogen deficient streams using hydrogen donor streams in a hydropyrolysis process |
Also Published As
Publication number | Publication date |
---|---|
DE50206118D1 (de) | 2006-05-11 |
EP1285903B1 (de) | 2006-03-22 |
DE10139726A1 (de) | 2003-02-27 |
ATE321014T1 (de) | 2006-04-15 |
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