EP2997113A1 - Procédé de purification de gaz de synthèse - Google Patents

Procédé de purification de gaz de synthèse

Info

Publication number
EP2997113A1
EP2997113A1 EP14728437.6A EP14728437A EP2997113A1 EP 2997113 A1 EP2997113 A1 EP 2997113A1 EP 14728437 A EP14728437 A EP 14728437A EP 2997113 A1 EP2997113 A1 EP 2997113A1
Authority
EP
European Patent Office
Prior art keywords
gas
residence time
synthesis gas
cooling
dust
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.)
Withdrawn
Application number
EP14728437.6A
Other languages
German (de)
English (en)
Inventor
Leonhard Baumann
Roland Möller
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.)
Ecoloop GmbH
Original Assignee
Ecoloop GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Ecoloop GmbH filed Critical Ecoloop GmbH
Publication of EP2997113A1 publication Critical patent/EP2997113A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D39/00—Filtering material for liquid or gaseous fluids
    • B01D39/14—Other self-supporting filtering material ; Other filtering material
    • B01D39/20—Other self-supporting filtering material ; Other filtering material of inorganic material, e.g. asbestos paper, metallic filtering material of non-woven wires
    • B01D39/2068—Other inorganic materials, e.g. ceramics
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/42—Auxiliary equipment or operation thereof
    • B01D46/44—Auxiliary equipment or operation thereof controlling filtration
    • B01D46/46—Auxiliary equipment or operation thereof controlling filtration automatic
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/006—Reducing the tar content by steam reforming
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/008—Reducing the tar content by cracking

Definitions

  • the present invention is concerned with a process for the purification of dust-containing synthesis gases which arise in Reakto ⁇ ren or shaft furnaces by carbothermic and / or eletr- rothermische processes and after leaving the reactor or the shaft furnace at elevated temperatures over physical separation methods of dust-like solids liberated and be cooled by means of a downstream heat exchanger.
  • the object of the present invention is to improve the existing process for the production of synthesis gas to the effect that a long filter life he ⁇ reaches and yet the synthesis gas is best possible freed from dusty impurities and any existing long-chain or aromatic hydrocarbons.
  • the object is achieved in that the dust-containing synthesis gas is led after leaving the reactor and before the liberation of dust-like solids in the presence of steam over a residence time in a method of the type described above, wherein the Diffe ⁇ ence of Gasendtemperatur (T3) of the Synthesis gas after suc-
  • CONFIRMATION COPY exemption from the dust-like solids and cooling to the maximum gas temperature in the residence time (T2) is set to at least 400 K.
  • the content of long-chain or aromatic hydrocarbons as components in the gas stream can be significantly reduced by the residence time line upstream of the filter, so that an effective filter can be used without the risk of clogging of this filter.
  • the final temperature of the synthesis gas is less than 100 ° C as a result of the desired deposition of water as a condensate, for example. 50 ° C. Accordingly, the maximum gas temperature in the residence time is significantly above 400 ° C, for example between 450 ° C and 750 ° C.
  • the dimensioning of the residence time span depends essentially on the volumes for which the installation in which the previously described method is carried out is dimensioned.
  • a quotient formed from the amount of synthesis gas produced per hour in standard cubic meters and the volume of the residence time segment in m 3 of a maximum of 10,000 may be mentioned.
  • the residence time section can be embodied in the form of a suitably dimensioned pipeline, which, for example, can also be helically formed to achieve suitable residence times or can also be widened to achieve a corresponding volume.
  • Residence times of the synthesis gas in the residence time range between 0.5 and 15 seconds have proven particularly expedient.
  • the proven, preferably the residence time is between 1.5 and 10 seconds and even more preferably between 2 and 8 seconds.
  • the set residence time is a compromise between the desire for as complete as possible reaction of the undesirable components and the desire for a high throughput, which, as mentioned, by appropriate design of the residence time this fact can be taken into account.
  • At least two mechanical shut-off devices are arranged one behind the other in the residence time section, the gas space between the shut-off devices being acted upon at least temporarily by an inert gas as barrier medium.
  • This measure may be necessary for safety purposes in order to prevent an explosive mixture from forming in the filter devices behind the residence time path.
  • the oxygen content in the synthesis gas at least one point in the residence time can be measured temporarily and / or continuously, with a safety measure may preferably be that the measured in the residence time oxygen content serves as a monitoring variable and this on reaching an upper limit automatically triggers the closing of the successively arranged mechanical shut-off devices in the residence time, whereby the formation of an explosive gas mixture in downstream filter housings is avoided.
  • a safety measure may preferably be that the measured in the residence time oxygen content serves as a monitoring variable and this on reaching an upper limit automatically triggers the closing of the successively arranged mechanical shut-off devices in the residence time, whereby the formation of an explosive gas mixture in downstream filter housings is avoided.
  • the liberation of the dust-like solids by filtration through temperature-resistant ceramic filter elements, which are installed in one or more filter housings, at temperatures above 300 ° C.
  • a quotient has formed from the amount of synthesis gas produced per hour in standard cubic meters and the volume of all filter housings in cubic meters of a maximum of 20 proved to be advantageous.
  • the synthesis gas is cooled by indirect cooling by means of a liquid cooling medium in one or more shell and tube heat exchangers, so that the resulting synthesis gas end temperature (T3) is below the already mentioned 100 ° C and the resulting condensates at least partially be separated from the gas phase.
  • condensates obtained at the cooling of the synthesis gas at an own temperature of below 100 ° C are at least partially metered into the synthesis gas stream before the synthesis gas is additionally cooled in the gas cooling by indirect cooling.
  • the dedusted and cooled synthesis gas is preferably conveyed by means of a gas conveyor arranged after the gas cooling, which sucks the synthesis gas out of the reactor or the shaft furnace, so that a pressure gradient is formed over the residence distance, the filter housings and the gas cooling, the difference between the pressure of the Synthesis gas at the beginning of the residence time and the pressure of the synthesis gas after gas cooling is at least 50 mbar to ensure the desired gas flow rate.
  • the carbonaceous materials for the purpose of gasification and additionally oxygen-containing gas are supplied in a stoichiometric amount as a gasifying agent, the total ⁇ in the reactor preferably less than 0.5 and more preferably less than 0.4 is.
  • alkaline substances are added to the dust-containing synthesis gas before entering the residence time and / or directly in the residence time. It has been shown that the thermal cleavage by exploiting catalytic effects, can be significantly favored where ⁇ with as alkaline substances preferably carbonates or hydroxides or oxides of the hydraulic ⁇ alkali or alkaline earth metals or mixtures of these substances are used.
  • FIG. 1 shows an advantageous embodiment of the method and is intended to explain this, but not limit.
  • Crude synthesis gas (1) which is formed, for example, in a gasification reactor (2), depending on the conditions in the reactor in addition to fly ash also contain long-chain or aromatic hydrocarbons.
  • the synthesis gas (1) is heated to a gas temperature (T2) of, for example, 600 ° C and in the presence of water vapor over a residence time (6), thereby achieving a thermal / chemical cleavage of these gas components.
  • T2 gas temperature
  • the filtration of the gas can be carried out, for example, by filtration through ceramic filter elements (3), it being advantageous if the gas temperature (Tl) after the filtration step is at least 300 ° C.
  • the gas temperature (Tl) after the filtration step is at least 300 ° C.
  • the tube bundle heat exchanger is usually acted upon on the outside of the tube by means of cooling water (10).
  • the thereby deposited condensates (11) may consist of different liquid phases.
  • a particularly preferred procedure can be achieved in that a countercurrent gasifier is used as the gasification reactor (2), which is flowed through from top to bottom by a bulk material moving bed (14) to which carbon-rich substances (15) are added prior to entry into the reactor ,
  • oxygen-containing gas (16) is metered in at the lower end of the reactor.
  • preference is given to establishing sub-stoichiometric ratios in the reactor, the total lambda being less than 0.5 and preferably less than 0.4.
  • alkaline substances (18) can be added to the synthesis gas (17) before entry into the residence time section (17) or directly into the residence time section (6).
  • the thermal decomposition can be significantly promoted by exploiting catalytic effects.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Ceramic Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Industrial Gases (AREA)

Abstract

L'invention concerne un procédé servant à purifier des gaz de synthèse (1) contenant des poussières, qui se forment dans des réacteurs ou des fours à cuve (2) par des procédés carbothermiques et/ou électrothermiques et qui sont libérés après avoir quitté le réacteur ou le four à cuve à des températures élevées par des procédés de séparation physiques (3) des solides sous forme de poussière (4) et sont refroidis au moyen d'un échangeur de chaleur (5) en aval. L'invention vise à obtenir une longue durée de filtrage avec une purification satisfaisante du gaz de synthèse. A cet effet, selon l'invention, le gaz de synthèse contenant de la poussière (1) est acheminé, après avoir quitté le réacteur (2) et avant la libération de solides sous forme de poussière en présence de vapeur d'eau, sur un parcours de durée de séjour (6). La différence de température finale du gaz (T3) du gaz de synthèse est ajustée après l'élimination réussie des solides sous forme de poussière et le refroidissement à la température de gaz maximale dans le parcours de durée de séjour (T2) à au moins 400 K.
EP14728437.6A 2013-05-16 2014-05-07 Procédé de purification de gaz de synthèse Withdrawn EP2997113A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013008422.9A DE102013008422A1 (de) 2013-05-16 2013-05-16 Verfahren zur Reinigung von Synthesegasen
PCT/EP2014/001223 WO2014183847A1 (fr) 2013-05-16 2014-05-07 Procédé de purification de gaz de synthèse

Publications (1)

Publication Number Publication Date
EP2997113A1 true EP2997113A1 (fr) 2016-03-23

Family

ID=50896213

Family Applications (1)

Application Number Title Priority Date Filing Date
EP14728437.6A Withdrawn EP2997113A1 (fr) 2013-05-16 2014-05-07 Procédé de purification de gaz de synthèse

Country Status (8)

Country Link
US (1) US20160168494A1 (fr)
EP (1) EP2997113A1 (fr)
JP (1) JP2016521310A (fr)
CN (1) CN105358662A (fr)
CA (1) CA2912272A1 (fr)
DE (1) DE102013008422A1 (fr)
WO (1) WO2014183847A1 (fr)
ZA (1) ZA201508403B (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITUB20154263A1 (it) * 2015-10-09 2017-04-09 Techinvest S R L Filtro-scambiatore per syngas

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE459584B (sv) * 1987-10-02 1989-07-17 Studsvik Ab Foerfarande foer foeraedling av raagas framstaelld ur ett kolhaltigt material
TWI241392B (en) * 1999-09-20 2005-10-11 Japan Science & Tech Agency Apparatus and method for gasifying solid or liquid fuel
DE102007062414B4 (de) 2007-12-20 2009-12-24 Ecoloop Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
CA2713391A1 (fr) * 2008-01-14 2009-07-23 Boson Energy Sa Procede de gazeification de biomasse et appareil de production de gaz de synthese presentant une teneur elevee en hydrogene
US8137655B2 (en) * 2008-04-29 2012-03-20 Enerkem Inc. Production and conditioning of synthesis gas obtained from biomass
WO2010054948A2 (fr) * 2008-11-12 2010-05-20 Basf Se Gazéification du charbon avec catalyse intégrée
DE102009038094B4 (de) * 2009-08-19 2015-11-12 Siemens Aktiengesellschaft Abhitzeverwertung nach Trennung von Rohgas und Schlacke in einem Flugstromvergaser
DE102011014345A1 (de) * 2011-03-18 2012-09-20 Ecoloop Gmbh Verfahren zur energieffizienten und umweltschonenden Gewinnung von Leichtöl und/oder Treibstoffen ausgehend von Roh-Bitumen aus Ölschifer und /oder Ölsanden

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2014183847A1 *

Also Published As

Publication number Publication date
JP2016521310A (ja) 2016-07-21
WO2014183847A1 (fr) 2014-11-20
DE102013008422A1 (de) 2014-11-20
CN105358662A (zh) 2016-02-24
ZA201508403B (en) 2016-10-26
US20160168494A1 (en) 2016-06-16
CA2912272A1 (fr) 2014-11-20

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