EP2313478A2 - Dispositif et procédé de dégazage de cendres - Google Patents

Dispositif et procédé de dégazage de cendres

Info

Publication number
EP2313478A2
EP2313478A2 EP09777501A EP09777501A EP2313478A2 EP 2313478 A2 EP2313478 A2 EP 2313478A2 EP 09777501 A EP09777501 A EP 09777501A EP 09777501 A EP09777501 A EP 09777501A EP 2313478 A2 EP2313478 A2 EP 2313478A2
Authority
EP
European Patent Office
Prior art keywords
gas
dust
exchange
synthesis
gas exchange
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Withdrawn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
EP09777501A
Other languages
German (de)
English (en)
Inventor
Stefan Hamel
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.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Uhde 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 Uhde GmbH filed Critical Uhde GmbH
Publication of EP2313478A2 publication Critical patent/EP2313478A2/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Withdrawn legal-status Critical Current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
    • 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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • 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
    • 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
    • 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
    • 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
    • C10K1/026—Dust removal by centrifugal forces
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2273/00—Operation of filters specially adapted for separating dispersed particles from gases or vapours
    • B01D2273/20—High temperature filtration
    • 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1696—Integration of gasification processes with another plant or parts within the plant with phase separation, e.g. after condensation

Definitions

  • the invention relates to a device for degassing dusts, as they frequently occur in the production of synthesis gas in coal gasification reactions, as syngas gas mixtures of different purity levels are called, which are used for various chemical syntheses and usually in addition to carbon monoxide and hydrogen still contain carbon dioxide, nitrogen, hydrogen sulfide and other components in varying compositions.
  • Degassing of the dusts is carried out so completely that the toxic gases contained in the dust pose no more danger to the environment.
  • the residual gases thus obtained can be collected by the apparatus and carried out of the system.
  • the device according to the invention it is possible to use the remaining heat contained in the dusts and cool the dusts obtained.
  • the dusts are depressurized by the apparatus from a high pressure level, which usually occurs in coal gasification reactions, to a normal, atmospheric pressure level.
  • the invention also relates to a method by which dusts can be purified from synthesis gases and completely or almost completely degassed.
  • the thermal gasification of solid fuels is carried out under elevated pressure and high tempera ture ⁇ with the aim of a synthesis raw gas to produce with high energy content and / or with ei ⁇ ner composition favorable for further chemical syntheses.
  • Syn ⁇ thesis crude gas loaded with fly ash which has its origin in the ash content of the fuel supplied.
  • the fly dust is in the form of particles that must be separated before further use.
  • a dry deposition for example in a cyclone or in a filter, the usually very fine-grained solid falls as a bed, before it is discharged from the pressure chamber.
  • there is gas in the void volume of the particle bed here crude synthesis gas which is discharged with the solid.
  • US 2007/0084117 A1 teaches a further synthesis gas synthesis process which successively passes the synthesis gas obtained from a coal gasification reactor through a system for mixing with a cooler foreign gas, a heat exchanger and a dust collector. separator leads.
  • the dust collector may be equipped with a purge gas supply device.
  • the subsequent dust collector behind the expansion unit can be present several times in order to achieve an improved throughput. As a result, batches of fly ash can be flowed through with a purge gas overlapping in time in order to remove the unwanted gases during the emptying and filling of the containers.
  • the known methods provide for expelling the remaining synthesis Rohgastician before a flow of the fly ash.
  • One of the main causes of the high time required in the known method is that due to the very fine particle sizes of the fly ash when flowing against gravity with increasing gas velocity usually form channels through which the gas breaks through. Due to this inhomogeneous flow, the time required to exchange the gas in the entire gap volume increases. Due to the fine particles and the resulting high flow resistance, there is a risk of bulk material compaction during flow against gravity, resulting in problems during emptying or further conveying out of the container.
  • the invention solves the problem of degassing a dust from a synthesis gas, which is produced by a gasification process, by a device containing
  • a main dust separator A main dust separator
  • a storage device for dust wherein • is the produced synthesis gas via a connecting line in a Hauptstaubabscheider from which a dedusted synthesis raw gas stream and a staubförmi- ger solid, which also includes synthesis raw gas in the gaps between the dust particles can be removed,
  • the dust-like solid is led into a combination container having devices with which it can be expanded to a lower pressure level, so that an exhaust gas is obtained and a smaller amount of gas remains in the void-containing solid,
  • a transport device for a solid is provided in a gas exchange device, the latter containing
  • the gas exchange container can be relieved to atmospheric pressure
  • the gas exchange device has an outlet opening for a solid which has been at least partially freed from synthesis crude gas
  • the gas exchange device has an upwardly directed delivery device in which an upward gas and solids flow is adjustable
  • the conveying device has an open cross section, a lower free opening and an upper free opening
  • the lower free opening of the conveying device is located within the gas exchange container near the bottom
  • the dust collector is connected so that it can be supplied from the gas exchange container with a gas-solid flow
  • the dust separator has a discharge device for an exhaust gas flow and a downward connection for a solid which has been freed from synthesis raw gas into the gas exchange container.
  • a heat exchanger is located, which is designed as a cooler. is formed and positioned so that its cooling surfaces have contact with the dust-like solid.
  • at least one such cooler is arranged in the gas exchange device.
  • a cooler is optionally arranged in the process flow in the connection between dust collector and gas exchange container or directly on the gas exchange container, combinations are also possible.
  • the storage device for dust has a pressure equalization line, which is connected to the dust separator of the gas exchange device, and gas exchange container and dust can form a structural unit.
  • the invention solves the problem of degassing a dust from a synthesis gas, which is produced by a gasification process, and usually contains as main constituents CO, H 2 , and ash and dust particles, further by a method, wherein
  • the synthesis gas produced is led via a connecting line into a main dust separator, in which most of the dust is separated,
  • the solids stream is passed, after the dust removal, into a combined container while maintaining the pressure level, in which it is depressurized to a lower pressure, so that an exhaust gas flow is obtained and a smaller amount of gas remains in the void volume,
  • the solid stream from the combination tank is conveyed pneumatically by means of conveying gas into a gas exchange device, and
  • the dust is cooled in the process flow in the connection between the dust collector and gas exchange container. It can also be provided that the dust is cooled in the gas exchange container.
  • the conveying density in the transport line between combination container and gas exchange container is less than 75% of the bulk density of the dust-like solid.
  • supplied exchange gas is discharged discontinuously or continuously together with at least part of the synthesis gas in the gap space from either the combination tank or the gas exchange container.
  • Supply and discharge can be carried out independently of each other both continuously and discontinuously, which is an advantage of the invention due to the process flexibility achieved in operation.
  • the exchange gas supplied to the gas exchange container is supplied to disposal together with at least part of the synthesis raw gas located in the gap space after separation from the circulating solid and after leaving the gas exchange device.
  • the gas released from the combined tank is disposed of.
  • the supplied exchange gas is supplied to a combustion reactor together with at least a portion of the synthesis raw gas located in the gap space after separation from the circulating solid and after leaving the gas exchange apparatus and the gas released from the combination tank is fed to a combustion reactor.
  • the supplied ⁇ exchange gas together with at least a portion of the present in the gap space synthesis raw gas after separation from the circulating solid and after leaving the gas exchange device or released from the combination tank gas or both gases first a gas storage for buffering and Homogenization be supplied.
  • the described apparatus and method offer the advantage of fast and thorough degassing of fly ash from a coal gasification process.
  • the time required for the degassing of fly ash can be significantly reduced.
  • FIG. 1 shows the entire part of the device which is provided for the degassing of the stowage behind the exit stub for synthesis gas.
  • 2 shows the gas exchange device 21 with the gas exchange container 10 and the associated dust separator 13.
  • FIG. 3 shows the gas exchange container 10 with an integrated dust separator 13.
  • Fly ash-containing, pressurized synthesis raw gas 1 is guided in the fly ash separator 3, which may be designed as a filter or cyclone. This gives a dedusted synthesis gas 2 and fly ash 4, which latter is passed into the combination tank 5. It is unavoidable that small amounts of the synthesis raw gas in the void volume of the particle bed get into the combination tank 5. In Kombi whatsoeverer 5, the still pressurized fly ash is relaxed to a lower pressure level. Then, by adding conveying gas 8, the charge of the solid matter 7 is conveyed via a pneumatic conveying line 9 into the gas exchange container 10 of the gas exchange device 21. For volume compensation of the conveyed from the combination container 5 solid and pressure retention in combination tank 5, which serves as a transmitting vessel in the fly ash discharge, replacement gas 6 is added to the combination tank 5.
  • replacement gas 11 is added here in such a way that an upward gas-solid flow 12 is established.
  • This gas-solids flow passes into a separator, in which the solid is separated from the gas, so that the solid 14 again goes downwards in the direction of the starting point, where by gas addition 11, the upward gas-solid flow 12 is generated.
  • a solid circulation is set, which can be controlled via the geometric design of the gas exchange container 10 and in particular via the gas addition 11.
  • the de-solidified gas leaves the gas exchange vessel 10 either in continuous or batch mode.
  • Fig. 2 is an external solid circulation, here is adjusted by adding exchange gas 11, the upward gas-solid flow 12 from the gas exchange container 10 out into a dust separator 13. There, the solid is separated from the gas, which consists of a mixture of supplied exchange gas 11 and the gas of the void volume of the particle bed. The gas mixture 18 is supplied for disposal. The separated solid flows in the direction of gravity downwards in the direction of the gas exchange container 10. In the downward flow is designed as banksü ⁇ bertrager Structure designed as a plate heat exchanger heat exchanger 15 to dissipate the heat of the solid.
  • Fig. 3 the same principle, but with internal circulation, represented, i. E. the circulating solids flow is within the gas exchange container 10.
  • the gas exchange container 10 of the device according to the invention is here equipped with an integrated dust separator 13.
  • Heat transfer surfaces are also provided to cool the solid.
  • two double-walled running walls in the form of jacket cooling are provided as a heat exchanger 15. The heat transfer surfaces should be immersed during operation in the circulating solid.
  • the combined container 5 is used to first depressurise the next batch received to a lower pressure level during the time that a batch is being treated in the gas exchange vessel 10, thereby evacuating gap space gas, and then using the remaining time the gas supply 6 back to a higher pressure level. to be tense and immediately relaxed again.
  • the covering causes a dilution of the synthesis crude gas fraction in the void volume, as a result of the expansion, part of the now present gas mixture is removed.
  • this process can be repeated several times, so that already a portion of the synthesis raw gas is expelled from the void volume before the solid charge is promoted for treatment in the gas exchange container 10. This reduces the number of solid cycles in the gas exchange container 10, which shortens the cycle times. As a result, larger quantities of fly ash per unit of time can be freed from the synthesis raw gas and cooled despite a single-circuit operation.
  • the container is referred to here as combination container 5, since it fulfills various functions.
  • it serves as a lock container to receive batchwise solid at process pressure level and to relax to a low pressure level, it also acts as a pre-purification stage to remove by cyclic loading and relaxing a portion of the raw synthesis gas in advance from the bed, and other he serves as a transmitting vessel for pneumatic conveying to the main cleaning stage in the gas exchange vessel.
  • the replacement gases 6 and 11 and also the conveying gas 8 may be made of inert gas such as e.g. Nitrogen exist, but also air, carbon dioxide or similar can be used. If the gas mixture stream 18, for example, fed to an afterburner, the use of air as the replacement gas 11 may be advantageous and also contributes to reducing the inert gas consumption.
  • inert gas such as e.g. Nitrogen exist, but also air, carbon dioxide or similar can be used.
  • a further advantageous process variant of the pre-purification stage is not to cycle the charge cyclically with replacement gas and then to relax, but to pressurize them with a continuous stream at a constant pressure.
  • the flash gas flow peaks would be omitted and the disposal unit for the streams of residual gases 18 and 19 would be applied from the pre-cleaning stage and from the main cleaning stage with continuous currents.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Industrial Gases (AREA)
  • Cyclones (AREA)
  • Nonmetallic Welding Materials (AREA)

Abstract

La présente invention concerne un dispositif de dégazage de cendres résultant de la production d'un gaz de synthèse par gazéification. Le dispositif comprend un séparateur de cendres principal (3), un récipient de combinaison (5), des moyens de dégazage et de refroidissement, ainsi qu'un dispositif collecteur de cendres (17). Le gaz de synthèse produit est transféré dans un séparateur de cendres principal (3) par un conduit de raccordement (1). Un courant de gaz de synthèse brut (2) dont les cendres ont été extraites et une matière solide (4) se présentant sous forme de cendre et contenant encore du gaz de synthèse brut dans les interstices entre les particules de cendre peuvent être retirés dudit séparateur de cendres principal. La matière solide (4) se présentant sous forme de cendre est transférée dans un récipient de combinaison (5) comprenant des dispositifs qui permettent de détendre la matière à un niveau de pression inférieur, de manière à obtenir un effluent gazeux (19) et de manière qu'il reste une faible quantité de gaz dans la matière solide contenant des interstices. Le dispositif comprend également un dispositif de transport permettant de transporter une matière solide (7) dans un dispositif d'échange gazeux (21) qui comporte un récipient d'échange gazeux (10), un séparateur de cendres (13) et un dispositif d'alimentation en gaz d'échange (11). Le récipient d'échange gazeux (10) peut être détendu à pression atmosphérique et le dispositif d'échange gazeux (21) présente une ouverture de sortie pour une matière solide libérée au moins partiellement par du gaz de synthèse brut, ainsi qu'un dispositif de transfert (12) orienté vers le haut, dans lequel un courant de gaz et de matière solide ascendant peut être commandé. Le dispositif de transfert (12) présente une section transversale ouverte, une ouverture inférieure libre et une ouverture supérieure libre. Un dispositif d'alimentation en gaz d'échange (11) dirigé dans l'ouverture inférieure libre est placé sous l'extrémité inférieure du dispositif de transfert (12). Le séparateur de cendres (13) présente un système d'évacuation (18) pour un courant d'effluent gazeux, ainsi qu'un raccord (14) dirigé vers le bas et destiné à conduire une matière solide libérée par le gaz de synthèse brut dans le récipient d'échange gazeux (10).
EP09777501A 2008-07-31 2009-07-29 Dispositif et procédé de dégazage de cendres Withdrawn EP2313478A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008035604A DE102008035604A1 (de) 2008-07-31 2008-07-31 Vorrichtung und Verfahren zur Entgasung von Stäuben
PCT/EP2009/005473 WO2010012454A2 (fr) 2008-07-31 2009-07-29 Dispositif et procédé de dégazage de cendres

Publications (1)

Publication Number Publication Date
EP2313478A2 true EP2313478A2 (fr) 2011-04-27

Family

ID=41461510

Family Applications (1)

Application Number Title Priority Date Filing Date
EP09777501A Withdrawn EP2313478A2 (fr) 2008-07-31 2009-07-29 Dispositif et procédé de dégazage de cendres

Country Status (13)

Country Link
US (1) US20110183276A1 (fr)
EP (1) EP2313478A2 (fr)
KR (1) KR20110049829A (fr)
CN (1) CN102137916B (fr)
AU (1) AU2009275394A1 (fr)
BR (1) BRPI0917207A8 (fr)
CA (1) CA2731966A1 (fr)
CU (1) CU23996B1 (fr)
DE (1) DE102008035604A1 (fr)
RU (1) RU2514960C2 (fr)
TW (1) TW201012918A (fr)
WO (1) WO2010012454A2 (fr)
ZA (1) ZA201100738B (fr)

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RU2516394C2 (ru) * 2012-07-19 2014-05-20 Открытое акционерное общество "Энергетический институт им. Г.М. Кржижановского" (ОАО ЭНИН) Установка для термической переработки твердых топлив
CN114262633B (zh) * 2021-12-06 2023-06-06 北京航天石化技术装备工程有限公司 一种高温含焦油热解气除尘装置与方法

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Also Published As

Publication number Publication date
RU2514960C2 (ru) 2014-05-10
DE102008035604A1 (de) 2010-02-04
US20110183276A1 (en) 2011-07-28
KR20110049829A (ko) 2011-05-12
CU20110023A7 (es) 2012-06-21
ZA201100738B (en) 2011-10-26
WO2010012454A3 (fr) 2010-08-05
CN102137916A (zh) 2011-07-27
BRPI0917207A8 (pt) 2016-07-05
CA2731966A1 (fr) 2010-02-04
AU2009275394A1 (en) 2010-02-04
CN102137916B (zh) 2014-07-30
CU23996B1 (es) 2014-04-24
WO2010012454A2 (fr) 2010-02-04
BRPI0917207A2 (pt) 2015-11-10
TW201012918A (en) 2010-04-01
RU2011107281A (ru) 2012-09-10

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