EP0161290A1 - Coal liquefaction process. - Google Patents
Coal liquefaction process.Info
- Publication number
- EP0161290A1 EP0161290A1 EP84904097A EP84904097A EP0161290A1 EP 0161290 A1 EP0161290 A1 EP 0161290A1 EP 84904097 A EP84904097 A EP 84904097A EP 84904097 A EP84904097 A EP 84904097A EP 0161290 A1 EP0161290 A1 EP 0161290A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- zone
- coal
- coking
- reaction product
- reaction
- 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
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
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
Definitions
- the invention relates to a process for liquefying coal, in which the ground coal is mixed with pulverizers to a pulp and liquefied under increased pressure and elevated temperature in a reaction zone in the presence of hydrogen and, if appropriate, catalyst.
- a process for liquefying coal has already become known, in which the coal to be processed is dried and finely ground, mixed with grinding oil, the coal pulp obtained is pumped to reaction pressure, first by heat exchange with part of the reaction products and then in a prerecessor ⁇ heated by supplying external heat to the light-off temperature of the liquefaction reaction and finally liquefied in a reaction zone in the presence of hydrogen and one or more suitable catalysts.
- the product fraction leaving the reaction zone is converted in a downstream hot separator into a vaporous top fraction of gases, water of reaction and distillate oils as well as into a solid fraction of the bottom from undegraded coal, ash, catalyst particles, and other high molecular weight substances which are difficult to hydrogenate, especially asphaltenes , and heavy oil disassembled.
- the entire coal to be processed must be dried in a special dryer using external heat.
- an amount of energy of about 0.1 Gcal is already required to dry a ton of coal.
- the coal has to be ground to a grain size of ⁇ 0.1 mm in a complex manner.
- the heat exchange for heating the coal pulp also proves to be very difficult.
- due to the viscosity of the coal pulp uniform application of heat to the heat exchanger surfaces is difficult to achieve.
- the further heating of the coal pulp in the preheater encounters difficulties because, due to the high temperatures already prevailing here, the coal suspended in the coal pulp swells very strongly. This leads to a further increase in the viscosity, so that in the end only a pulsating throughput of the coal slurry through the preheater connected with strong material output is possible. Pressure surges of up to 10 bar can occur.
- the desired yield of distillate oil also depends very much on the hydrogenation conditions (for example pressure, temperature) in the reaction zone.
- a satisfactory desti 11 oil can be obtained, for example over 50% based on the coal used, only with very harsh hydrogenation conditions with temperatures in the range of about 480 ° C and pressures above 300 bar. It is obvious that such conditions are associated with extraordinarily high investment costs and operating costs in a large-scale plant, with considerable effects on the economics of the process.
- the invention is based on the object of developing a method of the type mentioned at the outset in which the disadvantages described do not occur and which enables coal to be liquefied economically.
- reaction product leaving the reaction zone is fed to a coking zone and in that the hot gases and vapors withdrawing from the coking zone are cooled in heat exchange with the pulp to be heated.
- An essential idea of the invention is not to restrict the liquefaction of the coal to a reaction zone operated under harsh hydrogenation conditions, as in the known process, but to include a further coking zone in the oil production.
- the liquefaction can be directed in the reaction zone by lowering the pressure or the temperature, for example, so that initially primarily extract and only relatively little distillate oil are formed from the coal. A further large amount of distillate oil is then produced in the course of the coking.
- the pressure in the reaction zone is generally below 300 bar, preferably between about 150 and 250 bar.
- the coking of the reaction product withdrawing from the reaction zone is expediently carried out at temperatures between about 450 ° and 600 ° C., the temperature increase of the reaction product to be coked which may be necessary can be brought about by supplying external heat by means of a conventional tube furnace. Also by adding hydrogen e.g. in the form of coke oven gas, the quality and the yield of distillates in the coking zone can still be increased. To prevent coking in the course of heating the reaction product, it proves expedient to add a hydrogen-donate oil, in particular a higher-boiling fraction of the already hydrogen-refined oil gain, to the plant before it is heated.
- coking hot gases and vapors extracting from the zone below the respective coking temperature essentially these are desti ole oil vapors, to be cooled in the heat exchange with the fresh coal pulp to be treated in order to use the heat potential from the coking zone for heating the coal pulp.
- the coal pulp is heated in direct heat exchange, ie. H. through intimate mixing of the hot gases and vapors with the fresh coal pulp, which may already have been completely or partially pumped under pressure.
- direct heat exchange ie. H. through intimate mixing of the hot gases and vapors with the fresh coal pulp, which may already have been completely or partially pumped under pressure.
- all of the water contained in the coal is expelled, so that the coal is almost completely dried during this heat exchange.
- the hitherto customary, very complex drying in the course of coal preparation can thus be dispensed with completely or at least to a large extent if the feed coal has a high water content.
- An additional, very significant advantage is that, as a result of the strong heating of the coal in direct heat exchange with the hot product steams from the coking zone, more of the coal is easily removed. splitting gases, such as methane, CO 2 and formation water, are released. The coal to be fed to the reaction zone after the heat exchange is thus already largely degassed, so that fewer gases are formed in the reaction zone itself. This in turn leads to a further increase in the hydrogen pressure in the reactor and thus to an improvement in the reaction conditions.
- the heavy distillates contained in these vapors condense. With the fresh coal pulp, these distillates reach the reaction or coking zone again and are split up into the valuable product fractions naphtha and middle distillate. Also, the condensed heavy distillation are 'te well as solvent for the coal and tier ⁇ ren addition to a dilution of Kohlebreis. They in turn serve as "rubbing oil".
- the fresh coal pulp can therefore be added as a thick pulp with up to 90% solids content. This thick slurry can be conveyed into the zone of direct heat exchange in a simple manner by means of low-wear screw conveyors.
- the gases and vapors from the coking zone which are not condensed in the course of the direct heat exchange, essentially these are residual hydrogen, water vapor, low-boiling hydrocarbons and, in particular, hydrocarbons obtained as products in the naphtha and medium oils, as well as the gases and gases released when the coal is heated Vapors are separated from the heated coal pulp and fed to a corresponding treatment, your residual heat can possibly be used to heat the required fresh hydrogen or the hydrogen-containing gas.
- the entire reaction product withdrawing from the reaction zone can be fed to the coking zone.
- the hot separator which is usually downstream of the reaction zone is omitted.
- the reaction product reaches the coking zone immediately below the temperature of the reaction zone of approximately 470 ° to 490 ° C., ie a temperature which is already in the range of the coking temperature that the amount of heat still required for heating to the coking temperature is only small. Possibly. the device for further heating can even be dispensed with entirely. In such a procedure, the unused residual hydrogen contained in the reaction product can also be used directly in the coking zone.
- the gases and vapors still contained in the reaction product can also be present in a hot separator downstream of the reaction zone at somewhat lower temperatures, essentially residual hydrogen, methane and other gases and distillate late in the naphtha and medium oil range, are separated so that the volume flow to be fed to the coking zone is reduced accordingly.
- the gases and vapors separated in the hot separator can be fed directly to the direct heat exchange with the fresh coal pulp, so that the heat content of these gases and vapors can also be used here to heat the fresh coal pulp.
- a particularly high-quality coke is to be produced in the coking zone, e.g. an electrode coke for metallurgical purposes, it makes sense to separate the substances still contained in the reaction product, such as unused coal, ash and catalyst particles.
- the solid separation can be carried out in a known manner e.g. by filtration, sedimentation or centrifugation.
- reaction zone in two stages, the pressure of the second stage being higher than that of the first stage, which is preferably between about 10 and is 50 bar.
- the first reaction stage is below about
- the heating of the reaction product to the temperature of the coking zone can be achieved by admixing a hot, partially oxidized hydrocarbon-rich gas this is done.
- the hydrogen fraction 1 of this gas can then be used directly both to improve the coking and, if the reaction zone has two stages, to cover the hydrogen requirement in the first reaction zone.
- the hot, hydrogen-containing gas can be generated by partial oxidation of methane, with hydrogen and carbon monoxide being formed, among other things.
- the hot hydrogen-containing gas can also be obtained by partial oxidation, ie by gasification, of the coke obtained in the coking zone or, if before the coking Kung a residue separation has occurred, are generated by gasification of this residue.
- the admixture of the hydrogen-rich gas to the reaction product to be coked is expediently carried out at several, at least two points lying one behind the other in the direction of flow of the residue. This ensures a gradual, uniform heating of the residue, so that the coking temperature is only reached immediately before the reaction product is introduced into the coking zone. Possibly. it may also prove to be expedient to carry out the heating of the reaction product to be coked in two stages, with the hydrogen-containing hot gas being supplied in a tube furnace in a first stage and in a tube furnace in the second stage following the first stage.
- the coke accumulating in the coking zone is gasified, the raw gas obtained in the process is cleaned, partially converted and then at least partially a Fischer-Tropsch synthesis known per se for producing higher-boiling paraffinic hydrocarbons, in particular diesel oil , subjected.
- the plant can be operated in a simple manner by reducing the pressure and temperature in the reaction zone or the coking zone to less distillate gain, which means more coke for the gasification and the subsequent Fischer-Tropsch Synthesis occurs. Conversely, if there is an increased need for aroma - 15 -
- Table hydrocarbons for gasoline production the conditions for the treatment of coal in the reaction zone or the coking zone are tightened by increasing the pressure and temperature or by increasing the hydrogen supply, so that more distillate and less coke is obtained for gasification.
- a heavy oil fraction to grind the coal or petroleum residues resulting from the processing of petroleum, in particular hydrogenation residues still containing a catalyst.
- Such petroleum-derived grating oils are distinguished from coal oils by an increased hydrogen content l, which can be transferred to the coal to be treated even under particularly mild liquefaction conditions.
- petroleum hydrogenation residue which still contains catalyst it is also possible, if appropriate, to dispense with an additional catalyst for the coal treatment.
- the method according to the invention is not limited to the processing of hard coal or brown coal. Rather, the same advantages can also be treat their carbon-containing substances, such as, in particular, heavy oils derived from oil or oil sands or oil shale.
- the fresh coal pulp to be treated already mixed with a grinding oil and pumped to a pressure of about 20 bar, with a coal content of about 80 to 90% by weight, optionally together with a catalyst , fed to a mixer 2 and heated there to direct reaction exchange with hot gases and vapors, the origin of which is explained further below, to about the reaction temperature of about 400 ° C.
- the coal pulp is fed to a reaction zone 4 via a line 3 and there in Presence of hydrogen, which is introduced into the reaction zone 4 via a line 5, under relatively mild conditions, ie liquefied at a relatively low pressure of only about 200 bar and at a temperature of about 450 ° C.
- CMPI product is composed of a gaseous and a liquid solid phase.
- the hot gaseous phase which essentially contains the unused hydrogen, low-boiling hydrocarbons, such as methane, ethane and others, and distillates in the boiling range of naphtha and middle oil, is returned to the mixer 2 via a line 6, there intimately mixed with the fresh coal paste and cooled in the heat exchange with the coal paste.
- the liquid, solid-containing phase obtained in the reaction zone 4 consists essentially of coal extract, ie bitumen, and of distillates in the sieve area, predominantly of heavy oil. In addition, this phase contains solids such as unreacted coal, ash and unused catalyst.
- This liquid reaction product is fed via lines 7, 8, 9 and 10 to a furnace 11, heated there to a temperature of approximately 500 ° C. by indirect supply of external heat and then fed via lines 12, 13 and 14 into a coking zone 15.
- the liquid solid-containing product fraction is coked in the coking zone 15.
- coke, gases and vapors are produced, especially distillates in the boiling range of naphtha and co
- the product fraction to be coked can also be heated by directly admixing a hot hydrogen-containing gas mixture immediately before the product fraction enters the coking zone 15.
- the product fraction is introduced via lines 7, 8, 17, 13 and 14 directly into the coking zone 15, while the hydrogen-containing hot gas in a gas generator 18 by partial oxidation of methane or another hydrocarbon generated and admixed via line 19 of the product fraction to be coked.
- the partial oxidation can be controlled in such a way that on the one hand the oxidation of carbon to carbon monoxide produces sufficient heat to heat the fraction to be coked to coking temperature, but on the other hand also enough hydrogen is generated for the coking zone.
- the solids are separated from the coke before the reaction product is coked.
- the liquid solids-containing reaction product from the reaction zone 4 is first fed via lines 7 and 20 to a solids separation device 21, in which the solids are separated in a known manner, for example by filtration, sedimentation or else by centrifugation.
- the product fraction which is now largely freed of solids and is to be coked, is withdrawn via a line 22 from the solids separation device and, depending on the type of heating selected, via lines 9, 17, 13 and 14 or also via line 10 , the. Furnace 11 and lines 12, 13 and 14 of the coking zone 15 are fed.
- the solid-rich residue obtained in the solids separation device 21 is withdrawn from the system via a line 23. Possibly.
- This residue or at least part of the coke obtained in the coking zone 15 can be used in the gas generator 18 to produce the hydrogen-containing hot gas.
- the vapors generated in the coking zone 15 are withdrawn below the coking temperature of about 500 ° C. via a line 24 and likewise fed to the mixer 2.
- These vapors, together with the vapors from line 6, bring about the heating of the fresh coal pulp to about the light-off temperature of the reaction zone 4, so that, and this is an essential advantage of the proposed method, the supply of external heat in difficult-to-handle areas Heat exchangers for heating the fresh coal pulp can be dispensed with. In the course of the direct heat exchange of the said vapors with the coal pulp, almost all of the water is expelled from the coal, so that the energy-consuming drying of the coal in the course of its preparation can also be dispensed with.
- the gases and vapors obtained in the mixer 2 which essentially consist of residual hydrogen, water vapor, small amounts of low-boiling hydrocarbons, such as methane and ethane and others, and in particular the product distillates in the naphtha and middle oil range , are withdrawn from the system via a line 25 and a desti 11 further processing, not shown here,
- the coke obtained in the coking zone 15 is fed via a feed 26 into a gasifier 27, preferably a fixed bed gasifier, and gasified there to form a raw gas containing carbon monoxide and hydrogen.
- the required oxygen flows to the carburetor 27 via a line 28.
- the raw gas from the gasifier 26 is cleaned and converted in a downstream plant part 29 and then subjected to a known Fischer-Tropsch synthesis in a plant 30. Due to their paraffinic character, the hydrocarbons produced in this plant are particularly advantageous for the production of diesel fuel.
- the fresh coal pulp and / or the product fraction to be coked can also contain sulfur-binding substances, e.g. Calcium oxide or calcium carbonate can be added, and it has been shown that, due to their surface-active effect, these calcium compounds even contribute to a further increase in the oil yield.
- sulfur-binding substances e.g. Calcium oxide or calcium carbonate can be added, and it has been shown that, due to their surface-active effect, these calcium compounds even contribute to a further increase in the oil yield.
Abstract
Dans un procédé de liquéfaction du charbon avec accroissement de la pression et de la température dans une zone de réaction, on propose d'amener le produit de réaction quittant la zone de réaction à une zone de cokéfaction et de refroidir les gaz et les vapeurs qui s'y forment, et qui sont surtout des vapeurs de mazout, de préférence par échange de chaleur direct avec le brai de charbon frais. Les vapeurs et les gaz non-condensés lors de cet échange de chaleur sont retirés de l'installation en tant que produits finaux. Le procédé permet de déplacer partiellement la production d'huile de la zone de réaction à la zone de cokéfaction, si bien que la zone de réaction peut travailler à une basse pression. De plus, par l'échange de chaleur direct entre les vapeurs et le brai de charbon frais, une grande partie de la quantité de chaleur exotherme produite lors des réactions de liquéfaction peut être ramenée dans le procédé.In a process for liquefying coal with increasing pressure and temperature in a reaction zone, it is proposed to feed the reaction product leaving the reaction zone to a coking zone and to cool the gases and vapors which are formed there, and which are mainly fuel oil vapors, preferably by direct heat exchange with the fresh coal pitch. The vapors and gases not condensed during this heat exchange are removed from the installation as end products. The process allows the oil production to be partially moved from the reaction zone to the coking zone, so that the reaction zone can operate at low pressure. In addition, by the direct heat exchange between the vapors and the fresh coal pitch, much of the amount of exothermic heat produced during liquefaction reactions can be returned to the process.
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE3340041 | 1983-11-05 | ||
DE3340041 | 1983-11-05 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0161290A1 true EP0161290A1 (en) | 1985-11-21 |
EP0161290B1 EP0161290B1 (en) | 1987-08-12 |
Family
ID=6213546
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP84904097A Expired EP0161290B1 (en) | 1983-11-05 | 1984-11-03 | Coal liquefaction process |
Country Status (8)
Country | Link |
---|---|
US (1) | US4946583A (en) |
EP (1) | EP0161290B1 (en) |
JP (1) | JPS61500319A (en) |
AU (1) | AU575094B2 (en) |
CA (1) | CA1228315A (en) |
DE (1) | DE3465331D1 (en) |
WO (1) | WO1985001954A1 (en) |
ZA (1) | ZA848615B (en) |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0753965A (en) * | 1993-08-09 | 1995-02-28 | Nkk Corp | Liquefaction of coal |
US20080256852A1 (en) * | 2007-04-20 | 2008-10-23 | Schobert Harold H | Integrated process and apparatus for producing coal-based jet fuel, diesel fuel, and distillate fuels |
CN103254922B (en) * | 2013-04-17 | 2014-11-05 | 西安交通大学 | Two-stage coal direct liquefaction method and system |
IL227708A0 (en) * | 2013-07-29 | 2013-12-31 | S G B D Technologies Ltd | Processing combustible material methods and systems |
US9061953B2 (en) | 2013-11-19 | 2015-06-23 | Uop Llc | Process for converting polycyclic aromatic compounds to monocyclic aromatic compounds |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2852441A (en) * | 1954-10-22 | 1958-09-16 | Exxon Research Engineering Co | Conversion of hydrocarbons |
US3193486A (en) * | 1962-10-23 | 1965-07-06 | Sinclair Research Inc | Process for recovering catalyst particles in residual oils obtained in the conversion of hydrocarbon oils |
US3956101A (en) * | 1970-10-09 | 1976-05-11 | Kureha Kagaku Kogyo Kabushiki Kaisha | Production of cokes |
DE2654635B2 (en) * | 1976-12-02 | 1979-07-12 | Ludwig Dr. 6703 Limburgerhof Raichle | Process for the continuous production of hydrocarbon oils from coal by cracking pressure hydrogenation |
US4204943A (en) * | 1978-03-24 | 1980-05-27 | Exxon Research & Engineering Co. | Combination hydroconversion, coking and gasification |
US4213846A (en) * | 1978-07-17 | 1980-07-22 | Conoco, Inc. | Delayed coking process with hydrotreated recycle |
US4216074A (en) * | 1978-08-30 | 1980-08-05 | The Lummus Company | Dual delayed coking of coal liquefaction product |
DE3105030A1 (en) * | 1981-02-12 | 1982-09-02 | Basf Ag, 6700 Ludwigshafen | METHOD FOR THE CONTINUOUS PRODUCTION OF HYDROCARBON OILS FROM COAL BY PRESSURE HYDROGENATION IN TWO STAGES |
DE3141380A1 (en) * | 1981-10-17 | 1983-05-05 | GfK Gesellschaft für Kohleverflüssigung mbH, 6600 Saarbrücken | METHOD FOR HYDROGENATING COAL |
-
1984
- 1984-11-03 EP EP84904097A patent/EP0161290B1/en not_active Expired
- 1984-11-03 AU AU36141/84A patent/AU575094B2/en not_active Expired - Fee Related
- 1984-11-03 DE DE8484904097T patent/DE3465331D1/en not_active Expired
- 1984-11-03 WO PCT/DE1984/000233 patent/WO1985001954A1/en active IP Right Grant
- 1984-11-03 JP JP59504354A patent/JPS61500319A/en active Pending
- 1984-11-05 ZA ZA848615A patent/ZA848615B/en unknown
- 1984-11-05 CA CA000467059A patent/CA1228315A/en not_active Expired
-
1985
- 1985-05-20 US US06/744,554 patent/US4946583A/en not_active Expired - Fee Related
Non-Patent Citations (1)
Title |
---|
See references of WO8501954A1 * |
Also Published As
Publication number | Publication date |
---|---|
EP0161290B1 (en) | 1987-08-12 |
AU3614184A (en) | 1985-05-22 |
CA1228315A (en) | 1987-10-20 |
ZA848615B (en) | 1985-07-31 |
AU575094B2 (en) | 1988-07-21 |
US4946583A (en) | 1990-08-07 |
WO1985001954A1 (en) | 1985-05-09 |
DE3465331D1 (en) | 1987-09-17 |
JPS61500319A (en) | 1986-02-27 |
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