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.

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• 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)

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• 2013
  • 2013-05-16 DE DE102013008422.9A patent/DE102013008422A1/de not_active Withdrawn
• 2014
  • 2014-05-07 EP EP14728437.6A patent/EP2997113A1/de not_active Withdrawn
  • 2014-05-07 CN CN201480032857.XA patent/CN105358662A/zh active Pending
  • 2014-05-07 WO PCT/EP2014/001223 patent/WO2014183847A1/de active Application Filing
  • 2014-05-07 JP JP2016513248A patent/JP2016521310A/ja active Pending
  • 2014-05-07 CA CA2912272A patent/CA2912272A1/en not_active Abandoned
  • 2014-05-07 US US14/891,090 patent/US20160168494A1/en not_active Abandoned
• 2015
  • 2015-11-13 ZA ZA2015/08403A patent/ZA201508403B/en unknown

Non-Patent Citations (1)

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