EP0167702B1 - Verfahren zur Weiterverarbeitung von Schwelgas aus der Abfallpyrolyse - Google Patents

Verfahren zur Weiterverarbeitung von Schwelgas aus der Abfallpyrolyse Download PDF

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Publication number
EP0167702B1
EP0167702B1 EP85101873A EP85101873A EP0167702B1 EP 0167702 B1 EP0167702 B1 EP 0167702B1 EP 85101873 A EP85101873 A EP 85101873A EP 85101873 A EP85101873 A EP 85101873A EP 0167702 B1 EP0167702 B1 EP 0167702B1
Authority
EP
European Patent Office
Prior art keywords
gas
cooler
condensate
temperature
separated
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.)
Expired
Application number
EP85101873A
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German (de)
English (en)
French (fr)
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EP0167702A1 (de
Inventor
Hans Jürgen Dipl.-Ing. Wohner
Wilfried Pappmann
Peter Dr. Dipl.-Ing. Diemer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Krupp Koppers GmbH
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Krupp Koppers GmbH
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Publication of EP0167702A1 publication Critical patent/EP0167702A1/de
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    • 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
    • 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
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials

Definitions

  • the invention relates to a process for the further processing of the carbon-containing carbonization gas obtained in the pyrolysis of organic substances, in particular domestic waste, water and liquid hydrocarbons being separated from the gas.
  • the pyrolysis of waste containing organic substances is optionally carried out today with the addition of coal, preferably in closed rotary kilns with the exclusion of air.
  • the waste that is introduced is converted into smoldering coke by appropriate heating of the side walls, at the same time releasing a smoldering gas which, in addition to gaseous hydrocarbons, also contains liquid hydrocarbons and water as condensable components.
  • a smoldering gas which, in addition to gaseous hydrocarbons, also contains liquid hydrocarbons and water as condensable components.
  • the combustion of the smoldering gas produced without further gas treatment is therefore prohibited for economic reasons alone. Instead, efforts will be made to separate the liquid hydrocarbons contained in the gas, which are often also referred to as pyrolysis oil, and to use them separately.
  • DE-A 3 227 896 it is proposed in DE-A 3 227 896 to separate the carbonization gas obtained by condensation into the three fractions water, liquid hydrocarbons and gaseous hydrocarbons.
  • GB-PS 1 398 858 it is known to first subject the carbonization gas emerging from the pyrolysis reactor to hot dust removal and then to pre-cool it to a gas temperature which is above the dew point of the higher-boiling hydrocarbons contained in the gas.
  • DE-A 2 508 666 it is also known to wash the hot gases obtained in coal pressure gasification in several stages with coal tar oil, the gas being cooled down from stage to stage by the washing oil to such an extent that in the last washing stage the Evaporation point of the oil is higher than the temperature of the gas to be cleaned. The aim is to achieve an almost quantitative separation of the oil mist and vapors from the gas.
  • the three fractions resulting from the treatment of the carbonization gas emerging from the pyrolysis reactor can, of course, be further worked up or further processed in different ways. If the resulting gaseous fraction cannot be used directly on the system for indirect heating of internal consumers. the gas must be used for another recycling, e.g. B. for heating or synthesis purposes or for the generation of electrical energy. However, this requires a storable gas.
  • the invention is therefore based on the object of providing a process for the further processing of the carbonization gas obtained in the waste pyrolysis, in which the gas obtained as the end product can be stored over a longer period of time and, if appropriate, can also be fed into another gas supply network.
  • the liquid hydrocarbons present in the gas and the water should of course be separated as quantitatively as possible. At the same time, it should be possible to dispense with the use of external reagents in this process.
  • the pyrolysis reactor is provided with the reference number 1 in the flow diagram. As mentioned at the beginning, this can be a closed rotary kiln. However, it may also be a different type of reactor, such as. B. a fluidized bed reactor can be used. The details of the pyrolysis process need not be discussed here, however, since the process according to the invention is not tied to the use of certain process conditions in pyrolysis.
  • the carbonization gas at about 450 to 700 ° C. leaving the pyrolysis reactor is first introduced into the dust separator 2, in which most of the entrained coke dust is separated from the gas.
  • the dust collector 2 can be a type which is customary for this purpose, e.g. B. a cyclone act.
  • the gas After the hot dedusting, the gas reaches the gas quench 4 via line 3, to which a partial flow of the cold gas occurring behind the indirect cooler 22 is fed via line 5.
  • the hot gas coming from the pyrolysis reactor 1 is to be precooled to a temperature between 200 and 350 ° C. by direct contact with the returned cold gas, at which the gas is introduced via line 6 into the venturi scrubber 7.
  • the gas temperature should be set within the specified temperature range so that it is above the dew point of the higher-boiling hydrocarbons contained in the gas.
  • the temperature controller 8 which measures the temperature of the gas stream flowing in the line 6 and compares it with the predetermined desired value and, with a corresponding deviation from this, opens or throttles the valve 9 in the line 5 such that the supply of cold gas is above this line is increased or decreased accordingly until the desired temperature of the gas in line 6 has been reached.
  • the pre-cooled gas enters the venturi scrubber 7 from the line 6 from above, which is acted upon by line 10 with so-called self-condensate.
  • This self-condensate is a high-boiling hydrocarbon (heavy to medium oil) that is separated from the gas.
  • the self-condensate supplied via line 10 has a temperature of 100 to 200 ° C.
  • the fine dust removal of the gas takes place, which is caused on the one hand by the self-condensate that has been released and on the other hand by the condensation of the higher-boiling hydrocarbons.
  • the constituents separated from the gas are drawn off via line 11 into the so-called first separating tank 12, while the dedusted gas is introduced via line 13 into the direct cooler 14 from below.
  • the gas is cooled in direct contact with the self-condensate supplied via line 15 to a gas outlet temperature between 60 and 120 ° C.
  • the self-condensate supplied via line 15 has been cooled in the indirect cooler 16 to a temperature between 60 and 100 ° C.
  • the gas temperature in the direct cooler 14 is set so that it is above the dew point of the water vapor contained in the gas.
  • the gas emerging from the direct cooler 14 reaches the indirect cooler 22 via the line 17.
  • the gas outlet temperature in the line 17 is monitored and controlled by the temperature controller 18. This works on the same principle as the temperature controller 8 and actuates the valve 19, which is installed in the cooling water bypass line 20.
  • the cooling water supply to the indirect cooler 16 can be controlled and its performance can thus be influenced. This in turn makes it possible to influence the temperature of the self-condensate fed to the direct cooler 14 via the line 15 and thus to ensure the desired cooling effect in the direct cooler 14.
  • the higher-boiling hydrocarbons still present in the gas condense on the free surfaces of the cooled self-condensate.
  • the constituents separated from the gas are likewise introduced into the first separating container 12 via the line 21.
  • the gas from line 17 is introduced from above into the indirect cooler 22, in which it is cooled to a gas outlet temperature of 20 to 30 ° C.
  • the gas is simultaneously sprinkled with self-condensate, which is applied to the indirect cooler 22 via the line 24.
  • the constituents separated from the gas are withdrawn via line 25 and pass into the so-called second separating container 26.
  • the correspondingly cooled gas is withdrawn via line 27 from the direct cooler 22 and pressed by the gas suction device 28 into the indirect final cooler 29, in which it cools down to a final temperature between 0 and 5 ° C.
  • a partial stream of the gas in line 27 is branched off via line 5 and returned to gas quench 4.
  • the amount of this partial flow is, as described above, controlled by the temperature controller 8 with the aid of the valve 9.
  • the gas cooled in the indirect final cooler 29 is drawn off via the line 30 and fed to its further use or intermediate storage.
  • the low-water condensate separating in the final cooler 29 is drawn off by means of the pump 32 via the line 31.
  • a partial flow of this condensate can be fed back to the final cooler 29 via line 33 for flushing purposes, while the excess condensate is introduced via line 34 into the separating container 26.
  • the amount of condensate drawn off through line 34 is controlled by controller 35, which controls valve 36 as a function of the liquid level at the bottom of final cooler 29. If the liquid level rises above a predetermined setpoint, the valve 36 is automatically opened, while it is automatically closed when the liquid level falls below the setpoint.
  • the solid to liquid gas constituents (condensates) drawn off from the venturi washer 7 and the direct cooler 14 are separated into an oil-containing thick tar and an oil phase in the so-called first separating tank 12.
  • the separating container 12 can be a tar separator of a conventional type, as is also used in the treatment of coke oven gases.
  • the resulting oil-containing thick tar, which contains the dust deposited in the venturi washer 7, collects at the bottom of the separating container 12 and is discharged from the separating container 12 by means of the screw conveyor 37.
  • the pump 38 feeds it back via line 39 into the pyrolysis reactor 1, where it is also converted.
  • the oil phase on the other hand, which separates out as a lighter phase over the thick tar, is drawn off from the separating container 12 via the line 40 and pressed into the lines 10 and 15 by the pump 41, via which a re-application to the venturi washer 7 and the direct cooler 14 he follows.
  • the amount of the oil-containing thick tar drawn off is controlled by the controller 43 which, depending on the liquid level at the bottom of the direct cooler 14, actuates the speed controller 44 of the pump 38.
  • the controller 43 works in such a way that the speed of the pump 38 and thus its delivery rate is increased with increasing liquid level, while the speed and delivery rate of the pump 38 are throttled when the liquid level falls.
  • the liquid gas constituents (condensates) separated in the indirect cooler 22 are essentially a water-containing light oil fraction, which is separated into an oil and a water phase in the so-called second separating container 26.
  • the oil phase which separates out over the water phase is withdrawn from the separating tank 26 via the overflow 46 and the line 45 and is pressed into the line 24 by the pump 47. Via this line, the indirect cooler 22 is returned.
  • the line 24 is connected to the line 42 via the valve 48 connected so that excess oil can be removed from the circuit and drawn off through line 42. This is light oil with a boiling range of approx. 30 to 230 ° C.
  • the valve 48 is actuated by the controller 49, the control taking place as a function of the liquid level in the separating container 26 in the manner already described.
  • the water separated in the separating container 26 is pressed by the pump 50 into the line 51, via which it is removed from the process.
  • the water can be fed to a biological wastewater treatment plant or otherwise destroyed.
  • the controller 52 controls the drainage of water depending on the state of the water phase in the separating container 26 via the valve 53.
  • the oil fractions obtained in the individual process stages can also be drawn off separately. and be recycled if this is appropriate due to the operational circumstances.
  • the indirect coolers 16 and 22 are connected to one another by a common cooling water circuit.
  • the cooling water which may have been mixed with an antifreeze, is introduced via line 54 into the cooling coil 23 of the indirect cooler 22. From there it passes via line 55 into indirect cooler 16, from which it is withdrawn via line 56.
  • the removed cooling water can be reused after appropriate re-cooling.
  • the implementation of the method according to the invention is not tied to the cooler embodiments shown in the figure. Rather, other types of coolers can also be used.
  • the gas composition is changed as follows. While the partially dedusted gas in line 3 has a composition in the following range: is the composition of the purified gas withdrawn via line 30 in the following range:
  • This gas is fully storable even at low temperatures and can be used as heating gas without difficulty. Since the self-condensates obtained are also used for gas treatment in the method according to the invention, the use of external reagents can be dispensed with. The removal of the resulting thick tar is also not a problem in the process according to the invention, since it is returned to the pyrolysis reactor.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Combustion & Propulsion (AREA)
  • Industrial Gases (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP85101873A 1984-06-08 1985-02-21 Verfahren zur Weiterverarbeitung von Schwelgas aus der Abfallpyrolyse Expired EP0167702B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19843421393 DE3421393A1 (de) 1984-06-08 1984-06-08 Verfahren zur weiterverarbeitung von schwelgas aus der abfallpyrolyse
DE3421393 1984-06-08

Publications (2)

Publication Number Publication Date
EP0167702A1 EP0167702A1 (de) 1986-01-15
EP0167702B1 true EP0167702B1 (de) 1987-10-21

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ID=6237943

Family Applications (1)

Application Number Title Priority Date Filing Date
EP85101873A Expired EP0167702B1 (de) 1984-06-08 1985-02-21 Verfahren zur Weiterverarbeitung von Schwelgas aus der Abfallpyrolyse

Country Status (5)

Country Link
US (1) US4591366A (enrdf_load_stackoverflow)
EP (1) EP0167702B1 (enrdf_load_stackoverflow)
JP (1) JPS6128585A (enrdf_load_stackoverflow)
DD (1) DD237182A5 (enrdf_load_stackoverflow)
DE (2) DE3421393A1 (enrdf_load_stackoverflow)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7323594B2 (en) 1998-11-12 2008-01-29 Invitrogen Corporation Transfection reagents

Families Citing this family (24)

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Publication number Priority date Publication date Assignee Title
DE3609292A1 (de) * 1985-10-15 1987-04-16 Linde Ag Verfahren zum entfernen von verunreinigungen aus einem gas
DE3720258A1 (de) * 1987-06-19 1988-12-29 Marresearch Verfahren zur reduzierung der auf tanklagern, tankwagen-fuellstellen und schiffen anfallenden kohlenwasserstoff-emissionen und anlage zur durchfuehrung des verfahrens
DE3721475C1 (de) * 1987-06-30 1989-03-23 Asea Brown Boveri Anlage zur Pyrolyse von Abfallmaterial
DE3721450C1 (de) * 1987-06-30 1988-12-08 Asea Brown Boveri Verfahren zum Kuehlen von heissem Pyrolysegas
DE3721451C1 (de) * 1987-06-30 1988-12-08 Asea Brown Boveri Verfahren zum Betreiben einer Pyrolyseanlage
EP0308669A1 (de) * 1987-08-29 1989-03-29 Asea Brown Boveri Aktiengesellschaft Verfahren zum Verwerten von Halogenkohlenwasserstoffe enthaltendem Ausgangsmaterial
DE3835038A1 (de) * 1987-11-19 1990-04-19 Asea Brown Boveri Verfahren zum verringern der nebenprodukte bei der erzeugung vn pyrolysegas
WO1991005030A1 (en) * 1989-09-29 1991-04-18 Productcontrol Limited Method and apparatus for refinement or treatment of material
US5824122A (en) * 1992-10-23 1998-10-20 Siemans Aktiengesellschaft Process and apparatus for purifying flammable gas
DE19512850A1 (de) * 1995-04-06 1996-10-10 Veba Oel Technologie & Automatisierung Gmbh Verfahren zur Schwelgasentstaubung
DE19529536B4 (de) * 1995-08-11 2005-10-20 Schroeder Sascha Verfahren zur Aufbereitung und Konditionierung von Brenngas
DE19611119C2 (de) * 1996-03-21 2001-05-23 Sueddeutsche Kalkstickstoff Verfahren zur Reinigung von heißen, staub- und teerhaltigen Abgasen
CN1089270C (zh) * 1997-11-21 2002-08-21 刘兆彦 一种栅板式聚酯缩聚塔
NL1018803C2 (nl) * 2001-08-22 2003-02-25 Stichting Energie Werkwijze en stelsel voor het vergassen van een biomassa.
DE10159133A1 (de) * 2001-12-01 2003-06-26 Andreas Unger Gasreinigung mit konditionierten Kondensaten
JP4547244B2 (ja) * 2004-12-14 2010-09-22 有限会社 八太環境技術事務所 有機物のガス化装置
WO2011128990A1 (ja) * 2010-04-14 2011-10-20 Michimae Kiyoharu 乾留装置
US10767114B2 (en) * 2013-05-31 2020-09-08 Tolero Energy, Llc Pyrolysis system and method for bio-oil component extraction
JP6467805B2 (ja) * 2014-08-07 2019-02-13 新日鐵住金株式会社 タール利用設備の排ガス処理方法及び排ガス処理装置
JP6540645B2 (ja) * 2016-09-28 2019-07-10 Ｊｆｅスチール株式会社 有機物質の熱分解方法及び熱分解設備
US10793797B2 (en) 2017-08-16 2020-10-06 Praxair Technology, Inc. Integrated process and unit operation for conditioning a soot-containing syngas
JP2019147872A (ja) * 2018-02-26 2019-09-05 Ｊｆｅスチール株式会社 有機物質の熱分解方法及び熱分解設備
FI128804B (en) * 2019-06-10 2020-12-31 Neste Oyj METHOD FOR PROCESSING PLASTIC WASTE PYROLYL GAS
EP4043539A1 (de) * 2021-02-12 2022-08-17 Bernhard Grimm Vorrichtung und verfahren zur reinigung und/oder kondensation von pyrolysegas

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7323594B2 (en) 1998-11-12 2008-01-29 Invitrogen Corporation Transfection reagents

Also Published As

Publication number Publication date
DE3560795D1 (en) 1987-11-26
JPH0514755B2 (enrdf_load_stackoverflow) 1993-02-25
DD237182A5 (de) 1986-07-02
DE3421393A1 (de) 1985-12-12
EP0167702A1 (de) 1986-01-15
US4591366A (en) 1986-05-27
JPS6128585A (ja) 1986-02-08

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