WO2014044500A1 - Method for the treatment of a raw synthesis gas and a gas condensate - Google Patents

Method for the treatment of a raw synthesis gas and a gas condensate Download PDF

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Publication number
WO2014044500A1
WO2014044500A1 PCT/EP2013/067690 EP2013067690W WO2014044500A1 WO 2014044500 A1 WO2014044500 A1 WO 2014044500A1 EP 2013067690 W EP2013067690 W EP 2013067690W WO 2014044500 A1 WO2014044500 A1 WO 2014044500A1
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WO
WIPO (PCT)
Prior art keywords
gas
gas condensate
cooler
stream
washer
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.)
Ceased
Application number
PCT/EP2013/067690
Other languages
French (fr)
Inventor
Henrik Timmermann
Frederic Judas
Volker Deisinger
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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 Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of WO2014044500A1 publication Critical patent/WO2014044500A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • 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
    • C10K1/046—Reducing the tar content
    • 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
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • 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
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • This invention relates to a method for the treatment of a raw synthesis gas and a gas condensate from the gasification of carbonaceous feedstock carried out with oxygen and steam under elevated pressure and at elevated temperatures, wherein the raw synthesis gas initially is treated in a washer-cooler operated with gas condensate as washing and cooling medium, then in a waste heat boiler and then in at least one further cooler, wherein the gas condensate used in the washer-cooler is circulated via the waste heat boiler, wherein from this circuit a clarification stream is discharged and like the gas condensate formed in the at least one further cooler passed into a tar separator, and where- in a part of the gas condensate treated in the tar separator is recirculated as make-up stream into the gas condensate circuit of the washer-cooler.
  • the raw gas more exactly a raw synthesis gas comprising hydrogen and carbon oxides from the fixed-bed coal gasification, is introduced directly into the washer-cooler after leaving the pressure gasifier.
  • Said washer-cooler is operated with circulating gas con- densate as washing and cooling medium.
  • the raw synthesis gas is washed here, cooled and moistened.
  • the raw synthesis gas is passed into the so-called waste heat boiler.
  • the waste heat boiler is cooled further by indirect heat exchange, wherein moisture and other condensable substances are condensed out.
  • the raw synthesis gas is cooled further in at least one further heat exchanger, before it is handed over to further gas cleaning stages, which will not be discussed here in more detail.
  • the condensate formed in the washer-cooler, the waste heat boiler and the further heat exchangers will be referred to as gas condensate.
  • the gas condensate used in the washer-cooler is circulated via the waste heat boiler. From this circuit a clarification stream is discharged, which like the gas condensate formed in the further heat exchangers is passed into a tar separator. From the tar separator, a purified make-up stream is fed back into the circuit of the washer-cooler.
  • the gas condensate is cooled before introduction to a temperature of below 100 °C, in general to 80 °C, and depressurized from the pressure specified by the pressure gasification to atmospheric pressure.
  • An operating temperature of 80 °C was found to be useful, as above 80 °C an unnecessary quantity of steam would be generated during the depressurization of the gas condensate.
  • Below 80 °C the separation in the tar separator is more difficult, since the density differences between the constituents of the gas condensate are reduced with decreasing temperature.
  • the temperature of the make-up stream of likewise 80 °C resulting from this mode of operation leads to an undesired cooling of the gas condensate circuit of the washer-cooler.
  • the reduced temperature leads to the fact that the gas ab- sorbs less moisture.
  • less condensate is formed in the waste heat boiler, which due to a washing effect counteracts the soiling of the heat exchanger surfaces of the waste heat boiler.
  • less heat is transferred in the waste heat boiler, i.e. the heat transfer capacity of the waste heat boiler is utilized less.
  • Another problem of the method according to the prior art consists in that the heat which must be withdrawn from the gas condensate before introduction into the tar separator cannot be used further in the method itself and also in the upstream and downstream methods and plants. Therefore, the heat must be dissipated to the surroundings as heat loss, e.g. by means of a cooling tower. This heat loss should therefore be kept as low as possible. It is the object of the invention to provide a method which solves the above-described problems in an economic way.
  • the object underlying the invention is solved by a method with the features of claim 1 .
  • a particular aspect of the invention consists in that the heat exchange is carried out exclusively between the clarification stream and the make-up stream. Since the amount of gas condensate which is formed in the cooler or coolers downstream of the waste heat boiler is not very large, it is not worthwhile in some cases to pass this amount of gas condensate over a heat exchanger. The additional expenditure for the guidance of the corresponding material streams then is not justified with regard to the amount of recoverable energy. Consequently, there is obtained a conceptually simple method with satis- factory energy recovery.
  • the heat exchange between the clarification stream and the make-up stream is effected indirectly.
  • a make-up stream free from contamination is supplied to the washer-cooler.
  • a further particular aspect of the method consists in that the heat exchange is carried out by means of one or more heat exchangers constructed in the manner of a plate and/or spiral heat exchanger. Since the gas condensate coming from the raw synthesis gas treatment is greatly loaded with suspended matter, such as tar, oil and dust, plate and/or spiral heat exchangers are particularly useful at this point, since they can be cleaned with little expenditure of work.
  • Fig. 1 shows a preferred aspect of the method according to the invention.
  • the raw synthesis gas (1 ) originating from the pressure gasification of coal as carbonaceous feedstock is introduced into the washer-cooler (2) directly after leaving the pressure gasifier.
  • the gas is cooled, moistened and dedusted by direct con- tact with aqueous gas condensate (19, 20).
  • the raw synthesis gas and the gas condensate leave the washer-cooler (2) through a common conduit (3) and are introduced into the waste heat boiler (4).
  • gas and gas condensate are separated.
  • the waste heat boiler the gas is cooled indirectly by boiler feed water (21 ), which is evaporated to low-pressure steam (22), wherein further gas condensate is formed.
  • the gas is passed into the cooler (6) and further cooled down therein by indirect heat exchange, wherein boiler feed water (23) is converted into low-pressure steam (24). Subsequently, the gas is passed on via conduit (7) to further cooling and treatment steps, such as e.g. a gas cleaning by the Rectisol method (not shown).
  • the conduits (8) and (9) the gas condensate formed upon cooling the raw synthesis gas is discharged from the waste heat boiler and the downstream cooler, respectively.
  • the larger part of the gas condensate exiting from the waste heat boiler via conduit (8) is recirculated into the washer-cooler (2).
  • a clarification stream is withdrawn via conduit (25), in order to keep the content of tar, oil and solid par- tides constant.
  • the clarification stream (25) is passed over a plate heat exchanger (10), cooled in the process and joined with the gas condensate (9) discharged from the downstream cooler (6), cooled to 80 °C by means of a heat exchanger (1 1 ), depressur- ized to atmospheric pressure by means of a depressurizing device (12) and passed into a settling device, the so-called tar separator (13).
  • suspended matter such as oil (14), tar (15) and a sludge (16) containing solid particles are separated from the gas condensate and discharged from the tar separator.
  • the gas condensate cleaned in this way is withdrawn from the tar separator (13).
  • a part of this gas condensate is passed to the plate heat exchanger (10) via conduit (18), heated in the process, and via conduit (20) fed into the gas condensate circuit of the washer-cooler (2) as make-up stream.
  • the other part of the cleaned gas condensate withdrawn from the tar separator is supplied to the succeeding treatment stages (not shown) via conduit (26).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)

Description

Method for the Treatment of a Raw Synthesis Gas and a Gas Condensate
Field of the Invention
This invention relates to a method for the treatment of a raw synthesis gas and a gas condensate from the gasification of carbonaceous feedstock carried out with oxygen and steam under elevated pressure and at elevated temperatures, wherein the raw synthesis gas initially is treated in a washer-cooler operated with gas condensate as washing and cooling medium, then in a waste heat boiler and then in at least one further cooler, wherein the gas condensate used in the washer-cooler is circulated via the waste heat boiler, wherein from this circuit a clarification stream is discharged and like the gas condensate formed in the at least one further cooler passed into a tar separator, and where- in a part of the gas condensate treated in the tar separator is recirculated as make-up stream into the gas condensate circuit of the washer-cooler.
Prior art
Such method is known from the German Patent Specification DE 25 42 055 C3. Its basic features will be described below.
The raw gas, more exactly a raw synthesis gas comprising hydrogen and carbon oxides from the fixed-bed coal gasification, is introduced directly into the washer-cooler after leaving the pressure gasifier. Said washer-cooler is operated with circulating gas con- densate as washing and cooling medium. The raw synthesis gas is washed here, cooled and moistened. Subsequently, the raw synthesis gas is passed into the so-called waste heat boiler. Here, it is cooled further by indirect heat exchange, wherein moisture and other condensable substances are condensed out. Subsequent to the waste heat boiler, the raw synthesis gas is cooled further in at least one further heat exchanger, before it is handed over to further gas cleaning stages, which will not be discussed here in more detail. In the following, the condensate formed in the washer-cooler, the waste heat boiler and the further heat exchangers will be referred to as gas condensate. The gas condensate used in the washer-cooler is circulated via the waste heat boiler. From this circuit a clarification stream is discharged, which like the gas condensate formed in the further heat exchangers is passed into a tar separator. From the tar separator, a purified make-up stream is fed back into the circuit of the washer-cooler.
Since the tar separator is operated at atmospheric pressure, the gas condensate is cooled before introduction to a temperature of below 100 °C, in general to 80 °C, and depressurized from the pressure specified by the pressure gasification to atmospheric pressure. An operating temperature of 80 °C was found to be useful, as above 80 °C an unnecessary quantity of steam would be generated during the depressurization of the gas condensate. Below 80 °C, the separation in the tar separator is more difficult, since the density differences between the constituents of the gas condensate are reduced with decreasing temperature.
Unfavorably, however, the temperature of the make-up stream of likewise 80 °C resulting from this mode of operation leads to an undesired cooling of the gas condensate circuit of the washer-cooler. The reduced temperature leads to the fact that the gas ab- sorbs less moisture. As a result, less condensate is formed in the waste heat boiler, which due to a washing effect counteracts the soiling of the heat exchanger surfaces of the waste heat boiler. In addition, due to the lower temperature of the gas and the lower amount of condensate, less heat is transferred in the waste heat boiler, i.e. the heat transfer capacity of the waste heat boiler is utilized less.
Another problem of the method according to the prior art consists in that the heat which must be withdrawn from the gas condensate before introduction into the tar separator cannot be used further in the method itself and also in the upstream and downstream methods and plants. Therefore, the heat must be dissipated to the surroundings as heat loss, e.g. by means of a cooling tower. This heat loss should therefore be kept as low as possible. It is the object of the invention to provide a method which solves the above-described problems in an economic way.
Description of the Invention
The object underlying the invention is solved by a method with the features of claim 1 .
By increasing the temperature of the gas condensate, which is used as washing, cooling and moistening medium in the washer-cooler, in accordance with the invention, less cooling of the raw synthesis gas in the washer-cooler and a higher moisture absorption of the raw synthesis gas in the washer-cooler is achieved. The increased moisture of the raw synthesis gas leads to an improved washing effect in the waste heat boiler and due to increased condensation to a higher heat transfer in the waste heat boiler. In addition, the higher temperature of the raw synthesis gas and the resulting higher temperature difference to the boiler feed water used as cooling medium also leads to an increased heat transfer and hence to an increased conversion of boiler feed water into low- pressure steam.
A particular aspect of the invention consists in that the heat exchange is carried out exclusively between the clarification stream and the make-up stream. Since the amount of gas condensate which is formed in the cooler or coolers downstream of the waste heat boiler is not very large, it is not worthwhile in some cases to pass this amount of gas condensate over a heat exchanger. The additional expenditure for the guidance of the corresponding material streams then is not justified with regard to the amount of recoverable energy. Consequently, there is obtained a conceptually simple method with satis- factory energy recovery.
Preferably, the heat exchange between the clarification stream and the make-up stream is effected indirectly. In this way, a make-up stream free from contamination is supplied to the washer-cooler.
A further particular aspect of the method consists in that the heat exchange is carried out by means of one or more heat exchangers constructed in the manner of a plate and/or spiral heat exchanger. Since the gas condensate coming from the raw synthesis gas treatment is greatly loaded with suspended matter, such as tar, oil and dust, plate and/or spiral heat exchangers are particularly useful at this point, since they can be cleaned with little expenditure of work. Exemplary embodiment
Further developments, advantages and possible applications of the invention can also be taken from the following description of exemplary embodiments and drawings. All features described and/or illustrated form the invention per se or in any combination, independent of their inclusion in the claims or their back-reference.
The only Fig. 1 shows a preferred aspect of the method according to the invention. The raw synthesis gas (1 ) originating from the pressure gasification of coal as carbonaceous feedstock is introduced into the washer-cooler (2) directly after leaving the pressure gasifier. In said washer-cooler, the gas is cooled, moistened and dedusted by direct con- tact with aqueous gas condensate (19, 20). The raw synthesis gas and the gas condensate leave the washer-cooler (2) through a common conduit (3) and are introduced into the waste heat boiler (4). Here, gas and gas condensate are separated. In the waste heat boiler, the gas is cooled indirectly by boiler feed water (21 ), which is evaporated to low-pressure steam (22), wherein further gas condensate is formed. Via conduit (5), the gas is passed into the cooler (6) and further cooled down therein by indirect heat exchange, wherein boiler feed water (23) is converted into low-pressure steam (24). Subsequently, the gas is passed on via conduit (7) to further cooling and treatment steps, such as e.g. a gas cleaning by the Rectisol method (not shown). Via the conduits (8) and (9), the gas condensate formed upon cooling the raw synthesis gas is discharged from the waste heat boiler and the downstream cooler, respectively. Via conduit (19), the larger part of the gas condensate exiting from the waste heat boiler via conduit (8) is recirculated into the washer-cooler (2). From this circuit, a clarification stream is withdrawn via conduit (25), in order to keep the content of tar, oil and solid par- tides constant. The clarification stream (25) is passed over a plate heat exchanger (10), cooled in the process and joined with the gas condensate (9) discharged from the downstream cooler (6), cooled to 80 °C by means of a heat exchanger (1 1 ), depressur- ized to atmospheric pressure by means of a depressurizing device (12) and passed into a settling device, the so-called tar separator (13). Here, suspended matter such as oil (14), tar (15) and a sludge (16) containing solid particles are separated from the gas condensate and discharged from the tar separator. Via conduit (17), the gas condensate cleaned in this way is withdrawn from the tar separator (13). A part of this gas condensate is passed to the plate heat exchanger (10) via conduit (18), heated in the process, and via conduit (20) fed into the gas condensate circuit of the washer-cooler (2) as make-up stream. The other part of the cleaned gas condensate withdrawn from the tar separator is supplied to the succeeding treatment stages (not shown) via conduit (26).
Industrial Applicability
With the invention, an economic method is provided for the treatment of raw synthesis gas produced by pressure gasification of solid, carbonaceous feedstocks, which provides for a higher yield of the thermal energy contained in the raw synthesis gas and in the gas condensate.
List of Reference Numerals
(1 ) raw synthesis gas from pressure gasifier
(2) washer-cooler
(3) raw synthesis gas and gas condensate
(4) waste heat boiler
(5) raw synthesis gas
(6) cooler
(7) raw synthesis gas for the further treatment
(8) gas condensate
(9) gas condensate
(10) heat exchanger
(1 1 ) cooler
(12) depressurizing device
(13) tar separator
(14) oil draw
(15) tar draw
(16) solids draw
(17) gas condensate, cleaned
(18) gas condensate, cleaned, as make-up stream to the washer-cooler
(19) gas condensate, uncleaned to the washer-cooler
(20) gas condensate to the washer-cooler
(21 , 23) boiler feed water
(22, 24) low-pressure steam
(25) clarification stream
(26) gas condensate, cleaned, for the further treatment

Claims

Claims
A method for the treatment of a raw synthesis gas and a gas condensate from the gasification of carbonaceous feedstock carried out with oxygen and steam under elevated pressure and at elevated temperatures, wherein the raw synthesis gas initially is treated in a washer-cooler operated with gas condensate as washing and cooling medium, then in a waste heat boiler and then in at least one further cooler, wherein the gas condensate used in the washer-cooler is circulated via the waste heat boiler, wherein from this circuit a clarification stream is discharged and like the gas condensate formed in the at least one further cooler passed into a tar separator, and wherein a part of the gas condensate treated in the tar separator is recirculated as make-up stream into the gas condensate circuit of the washer-cooler, characterized in that between the make-up stream and the clarification stream and/or the gas condensate originating from at least one further cooler a heat exchange is carried out.
The method according to claim 1 , characterized in that the heat exchange is carried out exclusively between the clarification stream and the make-up stream.
The method according to claim 1 or 2, characterized in that the heat exchange between the clarification stream and the make-up stream is effected indirectly.
The method according to claim 3, characterized in that the heat exchange is carried out by means of one or more plate or spiral heat exchangers.
The method according to any of the preceding claims, characterized in that coal is used as carbonaceous feedstock.
PCT/EP2013/067690 2012-09-20 2013-08-27 Method for the treatment of a raw synthesis gas and a gas condensate Ceased WO2014044500A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102012108878.0A DE102012108878A1 (en) 2012-09-20 2012-09-20 Process for the treatment of a raw synthesis gas and a gas condensate
DE102012108878.0 2012-09-20

Publications (1)

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WO2014044500A1 true WO2014044500A1 (en) 2014-03-27

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PCT/EP2013/067690 Ceased WO2014044500A1 (en) 2012-09-20 2013-08-27 Method for the treatment of a raw synthesis gas and a gas condensate

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2607744A1 (en) * 1976-02-26 1977-09-08 Metallgesellschaft Ag PROCESS FOR GASIFICATION OF LARGE CHARACTERISTICS OF FUEL UNDER INCREASED PRESSURE FOR THE GENERATION OF LAKE GAS
DE2853989B1 (en) * 1978-12-14 1979-11-22 Metallgesellschaft Ag Process for the treatment of water-containing condensate from the cooling of the raw gas of the pressure gasification
DE2542055C3 (en) 1975-09-20 1985-08-22 Metallgesellschaft Ag, 6000 Frankfurt Process for the treatment of a raw gas from the pressurized gasification of coal
WO2010149173A2 (en) * 2009-06-26 2010-12-29 Dall Energy Holding Aps Method and system for cleaning of and heat recovery from hot gases

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3515484A1 (en) * 1985-04-30 1986-10-30 Metallgesellschaft Ag, 6000 Frankfurt METHOD FOR TREATING CONDENSATE FROM THE PRODUCT GAS OF GASIFYING SOLID FUELS

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2542055C3 (en) 1975-09-20 1985-08-22 Metallgesellschaft Ag, 6000 Frankfurt Process for the treatment of a raw gas from the pressurized gasification of coal
DE2607744A1 (en) * 1976-02-26 1977-09-08 Metallgesellschaft Ag PROCESS FOR GASIFICATION OF LARGE CHARACTERISTICS OF FUEL UNDER INCREASED PRESSURE FOR THE GENERATION OF LAKE GAS
DE2853989B1 (en) * 1978-12-14 1979-11-22 Metallgesellschaft Ag Process for the treatment of water-containing condensate from the cooling of the raw gas of the pressure gasification
WO2010149173A2 (en) * 2009-06-26 2010-12-29 Dall Energy Holding Aps Method and system for cleaning of and heat recovery from hot gases

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Publication number Publication date
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