WO1991009920A1 - Verfahren zum hydrieren eines kohlenstoffhaltigen einsatzgutes, insbesondere von kohle und/oder schweröl - Google Patents
Verfahren zum hydrieren eines kohlenstoffhaltigen einsatzgutes, insbesondere von kohle und/oder schweröl Download PDFInfo
- Publication number
- WO1991009920A1 WO1991009920A1 PCT/DE1990/000978 DE9000978W WO9109920A1 WO 1991009920 A1 WO1991009920 A1 WO 1991009920A1 DE 9000978 W DE9000978 W DE 9000978W WO 9109920 A1 WO9109920 A1 WO 9109920A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reaction zone
- heating
- reactor system
- main reaction
- reactor
- Prior art date
Links
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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
- C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
-
- 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/22—Non-catalytic cracking in the presence of hydrogen
Definitions
- the invention relates to a method for hydrogenating a feedstock containing hydrocarbon compounds, such as coal and / or heavy oil, by reaction with hydrogen at elevated pressure and temperature in a reaction system, the feedstock pumped under pressure being fed to the upper region of the reaction system and in this, from top to bottom, first passes through a heating or pre-reaction zone and then through a main reaction zone, while the hydrogen required passes the reaction system in countercurrent from bottom to top, and in which the hydrogenation products at the top and the residue in the lower region of the React ⁇ rsystems are deducted.
- hydrocarbon compounds such as coal and / or heavy oil
- the feedstock to be hydrogenated is pumped to reaction pressure and then fed into the upper region of the reactor.
- the feed passes through the reactor from top to bottom and is initially heated in a so-called heating or pre-reaction zone to approximately the light-off temperature of the hydrogenation.
- the majority of the hydrogenation reactions then take place in a subsequent main reaction zone.
- the hydrogenation is in the lower Area of the reactor system fed in and flows through from bottom to top.
- the hot product vapors and gases which arise in the main reaction zone and the excess hydrogen flow through the heating or pre-reaction zone contribute to the heating of the feed material and are then drawn off at the top of the reactor system.
- the non-hydrogenated residue is obtained in the lower region of the reactor system and is discharged from the plant at this point.
- the temperature of the main reaction zone e.g. be quenched with cold gas.
- the invention is based on the object of further developing a process for the hydrogenation of a carbon-containing feedstock, in particular coal and / or heavy oil, of the type mentioned at the outset such that, on the one hand, the outlay on equipment can be kept as low as possible and, at the same time, optimal use the exothermic excess heat follows.
- This object is achieved according to the invention in that part of the reactor content flowing from top to bottom in the reactor system is continuously returned from the main reaction zone to the heating or pre-reaction zone.
- Part of the reactor contents is expediently returned from the main reaction zone to the heating or pre-reaction zone by means of an agitator provided in the reactor system.
- an agitator provided in the reactor system.
- the temperature and thus reaction equilibrium in the reactor can be set in a simple manner by the proposed method.
- further exothermic excess heat is now transported from the main reaction zone into the heating or pre-reaction zone via the amount of liquid returned.
- the mass flows are adjusted so that the required temperature and thus reaction equilibrium is established in the reactor system. To set this required equilibrium, it is therefore neither necessary to supply external heat nor to destroy exothermic excess heat.
- the feed material pumped under pressure is divided into two partial streams, the a partial stream is introduced into the heating or pre-reaction zone and the second partial stream is introduced directly into the main reaction zone.
- the heating or pre-reaction zone now passes through a significantly smaller amount of feed material, so that correspondingly smaller amounts of heat are also required for heating to the starting temperature of the hydrogenation. Less exothermic excess heat therefore needs to be transported from the main reaction zone to the heating or heating zone. The excess heat remaining in the main reaction zone can be used directly for heating the second partial stream of the feed material.
- the setting of optimal hydrogenation conditions is made possible by the fact that the partial flow rates for the individual zones are regulated in dependence on the respectively predetermined target temperature of a zone, for example the heating or pre-reaction zone. Conventional control systems can be used, which need not be discussed further here.
- the transition region of both zones being expediently characterized by an annular cross-sectional constriction of the reactor system.
- the proposed feeding of the second partial flow and the narrowing of the cross-section in the transition area between the main reaction zone and the heating or pre-reaction zone ensure that predominantly fresh feed material, which is, however, already heated to hydrogenation temperatures, is fed into the heating or Pre-freak tion zone is returned. This then advantageously leads to an increase in the dwell time of the feed material fed in the second partial stream under hydrogenation conditions in the reactor system.
- the yield of distillate oils which are liquid under normal conditions can be increased further in that part of the hydrogen-rich gas obtained in the course of the preparation of the product vapors is returned to the heating or pre-reaction zone.
- the recirculated gas stream acts as a “strip gas” in this zone and contributes to the fact that dissolved distillate oils are expelled.
- the fresh hydrogen supplied to the reactor system can also be used to strip out residual amounts of distillate oil contained in the hydrogenation residue.
- the reactor system expediently has a further zone with a cross section which is narrower than the main reaction zone, in which the hydrogenated residue from the main reaction zone is brought into contact with the fresh hydrogen.
- the proposed method is particularly advantageously applicable to the hydrogenation of oils, such as Heavy oil or petroleum residues, or coal in each case alone or in mixtures.
- waste oils for example PCB-containing oils
- the waste oil is fed into the main reaction zone, either alone or in a suitable mixture with the feed.
- the waste oil is heated up very quickly to relatively high temperatures.
- the desired removal of the chlorine from the insert is thereby achieved.
- the feedstock to be hydrogenated in the present case a heavy oil, under reaction pressure of about 200 bar and a temperature of about 150 ° C. via a line 1 to a reactor system 2 operated according to the countercurrent principle, with one in the upper one Area of the reactor system provided heating or pre-reaction zone 3 and an adjoining main reaction zone 4.
- the transition area between zones 3 and 4 is characterized in the present case by an annular constriction 5 of the reactor cross-section.
- An agitator 6 serves - as schematically represented by the arrows - to continuously return part of the hot content of the main reaction zone 4 to the heating or pre-reaction zone 3, the exothermic excess heat carried along directly for heating the feed material in the heating or pre-reaction zone can be used, changes in the speed of the agitator and the angle of attack of the agitator blades in conjunction with a corresponding dimensioning of the annular constriction allow the quantity flow and thus the required heat flow to be adjusted relatively well.
- the required hydrogen for reaction is fed in the lower region of the reactor system 2 via a line 7 and flows through the reactor system 2 in countercurrent to the feed material from bottom to top.
- the resulting product vapors are drawn off at the top of the reactor system via line 8, while the residue containing solids leaves the system via line 9.
- the feedstock flowing in via line 1 is divided into two partial streams, one of which is fed via line 10 into the heating or pre-reaction zone 3 and the other via line 11 into the main reaction zone 4 is initiated immediately below the annular constriction 5.
- Valves 12 and 13 are provided in both lines, with which the respective flow rates can be regulated.
- the control is expediently carried out as a function of the target temperature, preferably the heating or pre-reaction zone 3, which is in the range of approximately 400 ° C. for the feed material in question.
- the proposed division of the feed material into the two partial streams 10 and 11 and the proposed quantity control make it possible to set and maintain the optimum steady state in the reactor in a simple manner.
- the heating is facilitated by the fact that only part of the feed material is fed to the heating or pre-reaction zone 3, so that smaller amounts of heat are required for heating in this part.
- reaction system 2 is expanded by a further zone 16 adjoining the main reaction zone 4, in which distillates still dissolved in the hydrogenated residue are now driven off using the fresh hydrogen as “stripping gas”.
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)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19893943036 DE3943036C2 (de) | 1989-12-27 | 1989-12-27 | Verfahren zum Hydrieren eines kohlenstoffhaltigen Einsatzgutes, insbesondere von Kohle und/oder Schweröl |
DEP3943036.7 | 1989-12-27 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1991009920A1 true WO1991009920A1 (de) | 1991-07-11 |
Family
ID=6396471
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/DE1990/000978 WO1991009920A1 (de) | 1989-12-27 | 1990-12-20 | Verfahren zum hydrieren eines kohlenstoffhaltigen einsatzgutes, insbesondere von kohle und/oder schweröl |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP0460159A1 (de) |
JP (1) | JPH04504879A (de) |
AU (1) | AU7038591A (de) |
CA (1) | CA2048662A1 (de) |
DE (1) | DE3943036C2 (de) |
WO (1) | WO1991009920A1 (de) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100338179C (zh) * | 2005-12-28 | 2007-09-19 | 煤炭科学研究总院 | 煤直接液化磁力刮刀环流反应器及其煤直接液化方法 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB327443A (en) * | 1928-12-31 | 1930-03-31 | William Ronald Tate | Method of destructive hydrogenation |
GB330025A (en) * | 1929-03-16 | 1930-06-05 | Thomas Girvan Hunter | Improved process and apparatus for the cracking or the destructive hydrogenation of oils, or suspensions of coal in oil |
US3891404A (en) * | 1973-03-09 | 1975-06-24 | Inst Gas Technology | Heavy oil hydrogasification process |
US4189374A (en) * | 1978-12-13 | 1980-02-19 | Gulf Oil Corporation | Coal liquefaction process employing internal heat transfer |
DE2945353A1 (de) * | 1979-11-09 | 1981-05-21 | Linde Ag, 6200 Wiesbaden | Verfahren und vorrichtung zur durchfuehrung stark exothermer reaktionen |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3013337A1 (de) * | 1980-04-05 | 1981-10-08 | Rheinische Braunkohlenwerke AG, 5000 Köln | Verfahren zur umwandlung von kohle und/oder hochsiedenden erndoel- oder teerrueckstaenden durch spaltende druckhydrierung |
DE3244251A1 (de) * | 1981-12-07 | 1983-06-09 | HRI, Inc., 08648 Lawrenceville, N.J. | Verfahren zur kohlehydrierung unter verwendung einer thermischen gegenstromreaktionszone |
US4510037A (en) * | 1983-12-23 | 1985-04-09 | Hri, Inc. | Hydrogenation process for solid carbonaceous feed materials using thermal countercurrent flow reaction zone |
-
1989
- 1989-12-27 DE DE19893943036 patent/DE3943036C2/de not_active Expired - Fee Related
-
1990
- 1990-12-20 WO PCT/DE1990/000978 patent/WO1991009920A1/de not_active Application Discontinuation
- 1990-12-20 EP EP19910901271 patent/EP0460159A1/de not_active Withdrawn
- 1990-12-20 CA CA 2048662 patent/CA2048662A1/en not_active Abandoned
- 1990-12-20 AU AU70385/91A patent/AU7038591A/en not_active Abandoned
- 1990-12-20 JP JP50166091A patent/JPH04504879A/ja active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB327443A (en) * | 1928-12-31 | 1930-03-31 | William Ronald Tate | Method of destructive hydrogenation |
GB330025A (en) * | 1929-03-16 | 1930-06-05 | Thomas Girvan Hunter | Improved process and apparatus for the cracking or the destructive hydrogenation of oils, or suspensions of coal in oil |
US3891404A (en) * | 1973-03-09 | 1975-06-24 | Inst Gas Technology | Heavy oil hydrogasification process |
US4189374A (en) * | 1978-12-13 | 1980-02-19 | Gulf Oil Corporation | Coal liquefaction process employing internal heat transfer |
DE2945353A1 (de) * | 1979-11-09 | 1981-05-21 | Linde Ag, 6200 Wiesbaden | Verfahren und vorrichtung zur durchfuehrung stark exothermer reaktionen |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100338179C (zh) * | 2005-12-28 | 2007-09-19 | 煤炭科学研究总院 | 煤直接液化磁力刮刀环流反应器及其煤直接液化方法 |
Also Published As
Publication number | Publication date |
---|---|
AU7038591A (en) | 1991-07-24 |
EP0460159A1 (de) | 1991-12-11 |
DE3943036A1 (de) | 1991-07-04 |
DE3943036C2 (de) | 1994-03-10 |
CA2048662A1 (en) | 1991-06-28 |
JPH04504879A (ja) | 1992-08-27 |
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