WO2018233872A1 - Process and plant for cooling synthesis gas - Google Patents
Process and plant for cooling synthesis gas Download PDFInfo
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- WO2018233872A1 WO2018233872A1 PCT/EP2018/025146 EP2018025146W WO2018233872A1 WO 2018233872 A1 WO2018233872 A1 WO 2018233872A1 EP 2018025146 W EP2018025146 W EP 2018025146W WO 2018233872 A1 WO2018233872 A1 WO 2018233872A1
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- feedwater
- synthesis gas
- plant
- condensate
- boiler feedwater
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Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
- C01B2203/0888—Methods of cooling by evaporation of a fluid
- C01B2203/0894—Generation of steam
Definitions
- the invention relates to a process and a plant for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas, which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous condensate formed being separated off, and treated in a plant for the catalytic conversion of carbon monoxide by means of water vapour into hydrogen and carbon dioxide.
- the synthesis gas produced After the synthesis gas produced has left the SMR, it is cooled by heat exchange with boiler feedwater.
- the boiler feedwater is vaporized here.
- the steam is used as feed steam for the SMR process and excess steam is discharged as export steam for use outside the SMR process.
- a synthesis gas consisting exclusively of hydrogen is to be produced as end product of the SMR process, then the synthesis gas is subsequently treated in a plant for catalytic conversion in which the carbon monoxide is converted by means of water vapour into hydrogen and carbon dioxide. This conversion is described in the abovementioned Ullmann volume on page 382 ff.
- the process of the invention concerns the further cooling of the synthesis gas which follows the previously described steps.
- the synthesis gas is firstly cooled further by heat exchange with the hydrocarbon-containing feed gas. This is followed by further cooling by heat exchange with degassed boiler feedwater, which is subsequently fed to the boiler, then by heating of the boiler feedwater degassing plant and for preheating the fresh boiler feedwater before the latter is introduced into the degassing plant. Degassing occurs purely physically as a result of heating of the boiler feedwater. The aqueous condensate formed in the synthesis gas up to this point is then separated as hot condensate from the synthesis gas stream.
- the synthesis gas is then cooled further almost to ambient temperature by means of an air cooler and the condensate formed, referred to as cold condensate, is separated off by means of a further condensate separator from the synthesis gas.
- the hot and cold condensate which has been separated off is used within the process for generating process steam.
- it is either kept separate from the fresh boiler feedwater and vaporised to form process steam in a separate boiler or it is introduced into the boiler feedwater degassing plant and mixed with the fresh boiler feedwater there.
- a disadvantage of this process according to the prior art is the high outlay in terms of the apparatus by means of which the boiler feedwater is, as described above, heated in two steps.
- a bypass conduit for the synthesis gas around the heat exchanger is required in order to regulate the preheating of the boiler feedwater.
- Dividing the synthesis gas stream between the stream going through the heat exchanger and the stream going through the bypass conduit requires a three-way valve or two mechanically connected regulating valves as are described in principle in the German first publication 1 950 055.
- the mechanical connection ensures that when one valve is closed, the other is opened to the same extent.
- These valves are very expensive.
- the piping system for the boiler feedwater has to be made safe by means of a safety valve to prevent overpressure caused by intrusion of synthesis gas through a possible leak in the preheating heat exchanger.
- blow- off conduit of the safety valve has to be connected to the flare system of the steam reforming plant, but this can allow boiler feedwater to get into the flare system and impair the function of the latter.
- This high outlay in terms of apparatus also requires additional construction height of the plant since a basic problem in the cooling of the synthesis gas is that the pipe for the synthesis gas has to be laid with a steady fall so that the condensate formed in the synthesis gas can flow down. Consequently, each cooling step results in additional height of the building and thus greater building costs.
- Process for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas, which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous condensate formed being separated off, and treated in a plant for the catalytic conversion of carbon monoxide by means of water vapour into hydrogen and carbon dioxide, comprising the following process steps:
- Plant of the invention Plant of the invention:
- Plant for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous condensate formed being separated off, and treated in a plant for the catalytic conversion of carbon monoxide by means of water vapour into hydrogen and carbon dioxide, comprising the following plant components: (a) heat exchanger for heat exchange between the synthesis gas and the hydrocarbon-containing feed gas,
- plant for degassing boiler feedwater comprising a feedwater vessel having a heat exchanger present therein for heat exchange between synthesis gas and the boiler feedwater and having at least one dome which is installed on the feedwater vessel and has internals for gas-liquid mass transfer, for example beds of random packing elements or structured packings, via which dome the boiler feedwater and/or the condensate separated off from the synthesis gas can be introduced into the feedwater vessel,
- the preheating of the boiler feedwater by heat exchange with the synthesis gas before the boiler feedwater enters the degassing plant, as is customary according to the prior art, is dispensed with according to the invention.
- the omission of the heat exchanger which has hitherto been required for this purpose saves building height.
- the preheating of the boiler feedwater is now effected in the feed dome of the degassing plant by heat exchange with water vapour ascending from the feedwater vessel. This type of preheating has, according to the prior art, been carried out only for the condensate which has been separated from the synthesis gas and recirculated to the degassing plant.
- the condensate separator for separating the condensate from the synthesis gas after heat exchange between synthesis gas and boiler feedwater becomes unnecesary.
- the omission of this condensate separator likewise saves building height.
- the subsequent air cooler in which the synthesis gas is cooled to about 40 °C by heat exchange with the surrounding air therefore also has to cool the condensate remaining in the synthesis gas and therefore has to be made larger.
- One preferred embodiment of the invention is characterized in that the boiler feedwater and the condensate separated off from the synthesis gas are each introduced via a separate feed dome into the feedwater vessel of the degassing plant.
- the throughput through each individual dome thus becomes smaller and the preheating of the boiler feedwater is improved.
- Fig. 1 a flow diagram of the prior art
- Fig. 2 a flow diagram of an illustrative embodiment of the invention.
- the synthesis gas 1 is cooled to a temperature of 360 °C by heat exchange and evaporation of boiler feedwater to give feed steam and export steam (not depicted in Fig. 1 ) and is introduced into heat exchanger 2. There, it transfers heat to the natural gas stream 3 which is fed as feed gas to steam reforming (not depicted).
- the synthesis gas 1 is then conveyed through the heat exchanger 4 and in this way heats the boiler feedwater 6 which has been degassed in the degassing plant 5.
- the boiler feedwater present in the feedwater vessel 7 is heated by the synthesis gas 1 by means of the heat exchanger 8.
- the performance of the heat exchanger 8 is regulated via the bypass 9 and the mechanically connected valves 10.
- the fresh boiler feedwater 12 is subsequently preheated by the synthesis gas 1 .
- the performance of the heat exchanger 1 1 is likewise regulated via a bypass 13 and mechanically connected valves 14.
- the synthesis gas 1 is in this way cooled to about 90°C. Since the synthesis gas 1 is under elevated pressure, it can intrude into the boiler feedwater conduit in the event of a leakage in the heat exchanger 1 1 , and the boiler feedwater conduit therefore has to be protected by a safety valve 16.
- the safety valve 16 blows, when actuated, the gas/water mixture 17 into the flare system (not shown).
- the condensate 18 formed up to this point is separated off in the separator 19.
- the synthesis gas 1 is cooled further to about 40 °C in air cooler 20 and then freed of condensate 22 in the separator 21 .
- the synthesis gas 1 is discharged for further treatment outside the process.
- the fresh boiler feedwater 15 and the condensates 18 and 22 are fed via the feed dome 23 into the degassing plant 5.
- the gases 24 driven off from the boiler feedwater are discharged into the atmosphere.
- a degassing plant 5 having two feed domes 23a and b is employed.
- the fresh boiler feedwater 12 is not preheated by heat exchange with the synthesis gas 1 before it is introduced into the degassing plant 5. Heating by the synthesis gas occurs exclusively in the feedwater vessel 7 by means of the heat exchanger 8.
- the condensate formed here in the synthesis gas 1 initially remains in the gas and is cooled together with the gas in the air cooler 20 and is only then separated off and introduced into the degassing plant 5.
- the omission of the heat exchanger 1 1 for preheating the fresh boiler feedwater 12 and the condensate separator 19 leads to a reduction in the construction height of the plant for carrying out the cooling of the synthesis gas.
- the heat exchanger 8 of the degassing plant 5 and the air cooler 20 have to be designed for higher performance.
- the invention allows a smaller construction height and thus a saving in building costs in the process for further cooling of synthesis gas, as is widely used in industry.
- the invention is thus industrially applicable.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Process and plant for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas, which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous condensate formed being separated off, with further cooling occurring and only two steps, namely heating of the plant for degassing of the boiler feedwater and cooling by heat exchange with the surrounding air, being provided for the further cooling, with only a small construction height being required due to the small number of cooling steps.
Description
Process and plant for cooling synthesis gas
Field of the invention
The invention relates to a process and a plant for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas, which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous condensate formed being separated off, and treated in a plant for the catalytic conversion of carbon monoxide by means of water vapour into hydrogen and carbon dioxide.
Prior art
Processes for producing synthesis gas containing hydrogen and carbon monoxide by means of catalytic steam reforming of a hydrocarbon-containing feed gas are known and are described, for example, in Ullmann's Encyclopedia of Industrial Chemistry, Sixth Edition, Vol. 15, Gas Production, Chapter 2. The feed gases, namely a hydrocarbon-containing gas such as natural gas and steam, are conveyed at elevated pressure, e.g. from 20 to 35 bar, and high temperature, e.g. from 800 to 950 °C, through externally heated, catalyst-filled reactor tubes. Here, the feed gases are converted into hydrogen-rich and carbon monoxide-rich synthesis gas. Such a reactor is frequently referred to as SMR and the process as SMR process, short for Steam Methane Reformer. It is very important in terms of the econmics of the
process to carry out very effective heat exchange between the synthesis gas exiting from the SMR and the feed gases.
After the synthesis gas produced has left the SMR, it is cooled by heat exchange with boiler feedwater. The boiler feedwater is vaporized here. The steam is used as feed steam for the SMR process and excess steam is discharged as export steam for use outside the SMR process. When a synthesis gas consisting exclusively of hydrogen is to be produced as end product of the SMR process, then the synthesis gas is subsequently treated in a plant for catalytic conversion in which the carbon monoxide is converted by means of water vapour into hydrogen and carbon dioxide. This conversion is described in the abovementioned Ullmann volume on page 382 ff.
The process of the invention concerns the further cooling of the synthesis gas which follows the previously described steps.
Here, the synthesis gas is firstly cooled further by heat exchange with the hydrocarbon-containing feed gas. This is followed by further cooling by heat exchange with degassed boiler feedwater, which is subsequently fed to the boiler, then by heating of the boiler feedwater degassing plant and for preheating the fresh boiler feedwater before the latter is introduced into the degassing plant. Degassing occurs purely physically as a result of heating of the boiler feedwater. The aqueous condensate formed in the synthesis gas up to this point is then separated as hot condensate from the synthesis gas stream. The synthesis gas is then cooled further almost to ambient temperature by means of an air cooler and the condensate formed, referred to as cold condensate, is separated off by means of a further condensate separator from the synthesis gas. The hot and cold condensate which has been separated off is used within the process for generating process steam. Depending on the purity of the condensate and the purity requirements which the export steam has to meet, it is either kept separate from the fresh boiler feedwater and vaporised to form process steam in a separate boiler or it is introduced into the boiler feedwater degassing plant and mixed with the fresh boiler feedwater there.
A disadvantage of this process according to the prior art is the high outlay in terms of the apparatus by means of which the boiler feedwater is, as described above, heated in two steps. Here, a bypass conduit for the synthesis gas around the heat exchanger is required in order to regulate the preheating of the boiler feedwater. Dividing the synthesis gas stream between the stream going through the heat exchanger and the stream going through the bypass conduit requires a three-way valve or two mechanically connected regulating valves as are described in principle in the German first publication 1 950 055. The mechanical connection ensures that when one valve is closed, the other is opened to the same extent. These valves are very expensive. Furthermore, the piping system for the boiler feedwater has to be made safe by means of a safety valve to prevent overpressure caused by intrusion of synthesis gas through a possible leak in the preheating heat exchanger. The blow- off conduit of the safety valve has to be connected to the flare system of the steam reforming plant, but this can allow boiler feedwater to get into the flare system and impair the function of the latter. This high outlay in terms of apparatus also requires additional construction height of the plant since a basic problem in the cooling of the synthesis gas is that the pipe for the synthesis gas has to be laid with a steady fall so that the condensate formed in the synthesis gas can flow down. Consequently, each cooling step results in additional height of the building and thus greater building costs.
Description of the invention
It is therefore an object of the invention to provide a process and a plant in which fewer cooling steps and therefore lower costs for equipment and buildings are required.
The object is achieved by the invention according to the features of Claims 1 and 3.
Process of the invention :
Process for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas, which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous
condensate formed being separated off, and treated in a plant for the catalytic conversion of carbon monoxide by means of water vapour into hydrogen and carbon dioxide, comprising the following process steps:
(a) heat exchange of the synthesis gas with the hydrocarbon-containing feed gas, (b) introduction of boiler feedwater into a degassing plant comprising a feedwater vessel, with the boiler feedwater not being preheated by heat exchange with the synthesis gas before introduction into the degassing plant, the boiler feedwater flowing through a dome installed on the feedwater vessel in countercurrent to water vapour ascending from the feedwater vessel into the feedwater vessel to effect preliminary degassing of the boiler feedwater and the water vapour being discharged together with the gases taken up from the feedwater from the degassing plant and the process for further treatment,
(c) heat exchange of the synthesis gas with the boiler feedwater which has been degassed in the degassing plant,
(d) heat exchange of at least part of the synthesis gas with the boiler feedwater present in the feedwater vessel of the degassing plant,
(e) heat exchange of the synthesis gas with the surrounding air,
(f) separation of condensate from the synthesis gas and introduction of the condensate into the degassing plant, with the condensate flowing through a dome installed on the feedwater vessel in countercurrent to water vapour ascending from the feedwater vessel into the feedwater vessel to effect preliminary degassing and the water vapour being discharged together with the gases taken up from the condensate from the degassing plant and from the process for further treatment,
(g) further conveying of the synthesis gas to further treatment outside the process.
Plant of the invention:
Plant for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas, which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous condensate formed being separated off, and treated in a plant for the catalytic conversion of carbon monoxide by means of water vapour into hydrogen and carbon dioxide, comprising the following plant components:
(a) heat exchanger for heat exchange between the synthesis gas and the hydrocarbon-containing feed gas,
(b) heat exchanger for heat exchange between the synthesis gas and the degassed boiler feedwater,
(c) plant for degassing boiler feedwater, comprising a feedwater vessel having a heat exchanger present therein for heat exchange between synthesis gas and the boiler feedwater and having at least one dome which is installed on the feedwater vessel and has internals for gas-liquid mass transfer, for example beds of random packing elements or structured packings, via which dome the boiler feedwater and/or the condensate separated off from the synthesis gas can be introduced into the feedwater vessel,
(d) heat exchanger for heat exchange of the synthesis gas with the surrounding air,
(e) condensate separator for separating condensate from the synthesis gas,
(f) a pipe for feeding the boiler feedwater from the boiler feedwater production which is not part of the plant to the degassing plant (c), with the pipe being laid in such a way that it opens into the dome which serves to supply the boiler feedwater to be degassed to the feedwater vessel of the degassing plant,
(g) pipe for transfer of the condensate from the condensate separator (e) to the degassing plant (c), with the pipe being laid in such a way that it opens into the dome which serves to supply the condensate to the feedwater vessel.
The preheating of the boiler feedwater by heat exchange with the synthesis gas before the boiler feedwater enters the degassing plant, as is customary according to the prior art, is dispensed with according to the invention.The omission of the heat exchanger which has hitherto been required for this purpose saves building height. The preheating of the boiler feedwater is now effected in the feed dome of the degassing plant by heat exchange with water vapour ascending from the feedwater vessel. This type of preheating has, according to the prior art, been carried out only for the condensate which has been separated from the synthesis gas and recirculated to the degassing plant. To introduce the heat energy now additionally required for steam generation, the area of the heat exchanger installed in the feedwater vessel is correspondingly increased. Furthermore, according to the
invention, the condensate separator for separating the condensate from the synthesis gas after heat exchange between synthesis gas and boiler feedwater becomes unnecesary. The omission of this condensate separator likewise saves building height. The subsequent air cooler in which the synthesis gas is cooled to about 40 °C by heat exchange with the surrounding air therefore also has to cool the condensate remaining in the synthesis gas and therefore has to be made larger.
Preferred embodiments of the invention
One preferred embodiment of the invention is characterized in that the boiler feedwater and the condensate separated off from the synthesis gas are each introduced via a separate feed dome into the feedwater vessel of the degassing plant. The throughput through each individual dome thus becomes smaller and the preheating of the boiler feedwater is improved. Working example
Further features, advantages and possible uses of the invention may be derived from the following description of working examples and the drawings. Here, all features described and/or depicted on their own or in any combination form the subject matter of the invention, regardless of the way in which they are summarized in the claims or their back references.
The process of the invention will be explained below with the aid of the drawings Fig. 1 and 2. The drawings show: Fig. 1 a flow diagram of the prior art,
Fig. 2 a flow diagram of an illustrative embodiment of the invention.
Fig. 1 :
The synthesis gas 1 is cooled to a temperature of 360 °C by heat exchange and evaporation of boiler feedwater to give feed steam and export steam (not depicted in Fig. 1 ) and is introduced into heat exchanger 2. There, it transfers heat to the natural gas stream 3 which is fed as feed gas to steam reforming (not depicted). The
synthesis gas 1 is then conveyed through the heat exchanger 4 and in this way heats the boiler feedwater 6 which has been degassed in the degassing plant 5. The boiler feedwater present in the feedwater vessel 7 is heated by the synthesis gas 1 by means of the heat exchanger 8. The performance of the heat exchanger 8 is regulated via the bypass 9 and the mechanically connected valves 10. The fresh boiler feedwater 12 is subsequently preheated by the synthesis gas 1 . The performance of the heat exchanger 1 1 is likewise regulated via a bypass 13 and mechanically connected valves 14. The synthesis gas 1 is in this way cooled to about 90°C. Since the synthesis gas 1 is under elevated pressure, it can intrude into the boiler feedwater conduit in the event of a leakage in the heat exchanger 1 1 , and the boiler feedwater conduit therefore has to be protected by a safety valve 16. The safety valve 16 blows, when actuated, the gas/water mixture 17 into the flare system (not shown). The condensate 18 formed up to this point is separated off in the separator 19. The synthesis gas 1 is cooled further to about 40 °C in air cooler 20 and then freed of condensate 22 in the separator 21 . The synthesis gas 1 is discharged for further treatment outside the process.
The fresh boiler feedwater 15 and the condensates 18 and 22 are fed via the feed dome 23 into the degassing plant 5. The gases 24 driven off from the boiler feedwater are discharged into the atmosphere.
Fig. 2
In this illustrated embodiment of the invention, a degassing plant 5 having two feed domes 23a and b is employed. The use of two domes, one for the introduction of the fresh boiler feedwater 12 and one for the introduction of the condensate 22 separated off from the synthesis gas, makes it possible to produce a larger contact area between the liquids to be degassed which are introduced and the steam flowing in countercurrent to these from the feedwater vessel. According to the invention, the fresh boiler feedwater 12 is not preheated by heat exchange with the synthesis gas 1 before it is introduced into the degassing plant 5. Heating by the synthesis gas occurs exclusively in the feedwater vessel 7 by means of the heat exchanger 8. The condensate formed here in the synthesis gas 1 initially remains in the gas and is
cooled together with the gas in the air cooler 20 and is only then separated off and introduced into the degassing plant 5. The omission of the heat exchanger 1 1 for preheating the fresh boiler feedwater 12 and the condensate separator 19 leads to a reduction in the construction height of the plant for carrying out the cooling of the synthesis gas. In return, the heat exchanger 8 of the degassing plant 5 and the air cooler 20 have to be designed for higher performance.
Industrial applicability
The invention allows a smaller construction height and thus a saving in building costs in the process for further cooling of synthesis gas, as is widely used in industry. The invention is thus industrially applicable.
List of reference numerals
1 Synthesis gas
2 Heat exchanger
3 Natural gas
4 Heat exchanger
5 Degassing plant
6 Boiler feedwater, degassed
7 Feedwater vessel
8 Heat exchanger
9 Bypass
10 Valves, mechanically connected
1 1 Heat exchanger
12 Boiler feedwater, fresh
13 Bypass
14 Valves, mechanically connected
15 Boiler feedwatwer, fresh, preheated
16 Safety valve
17 Gas-water mixture
18 Condensate
19 Condensate separator
20 Air cooler
21 Condensate separator
22 Condensate
23 a, b Feed dome
24 Gases driven off
Claims
1 . Process for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas, which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous condensate formed being separated off, and treated in a plant for the catalytic conversion of carbon monoxide by means of water vapour into hydrogen and carbon dioxide, comprising the following process steps:
(a) heat exchange of the synthesis gas with the hydrocarbon-containing feed gas,
(b) introduction of boiler feedwater into a degassing plant comprising a feedwater vessel, with the boiler feedwater not being preheated by heat exchange with the synthesis gas before introduction into the degassing plant, the boiler feedwater flowing through a dome installed on the feedwater vessel in countercurrent to water vapour ascending from the feedwater vessel into the feedwater vessel to effect preliminary degassing of the boiler feedwater and the water vapour being discharged together with the gases taken up from the feedwater from the degassing plant and the process for further treatment,
(c) heat exchange of the synthesis gas with the boiler feedwater which has been degassed in the degassing plant,
(d) heat exchange of at least part of the synthesis gas with the boiler feedwater present in the feedwater vessel of the degassing plant,
(e) heat exchange of the synthesis gas with the surrounding air,
(f) separation of condensate from the synthesis gas and introduction of the condensate into the degassing plant, with the condensate flowing through a dome installed on the feedwater vessel in countercurrent to water vapour ascending from the feedwater vessel into the feedwater vessel to effect preliminary degassing and the water vapour being discharged together with the gases taken up from the condensate from the degassing plant and from the process for further treatment, (g) further conveying of the synthesis gas to further treatment outside the process.
2. Process according to Claim 1 , characterized in that boiler feedwater and the condensate are each introduced via a separate dome into the feedwater vessel of the degassing plant.
3. Plant for cooling a synthesis gas produced by catalytic steam reforming of a hydrocarbon-containing feed gas, which synthesis gas has been cooled by heat exchange with boiler feedwater to convert the latter into steam, with the aqueous condensate formed being separated off, and treated in a plant for the catalytic conversion of carbon monoxide by means of water vapour into hydrogen and carbon dioxide, comprising the following plant components:
(a) heat exchanger for heat exchange between the synthesis gas and the hydrocarbon-containing feed gas,
(b) heat exchanger for heat exchange between the synthesis gas and the degassed boiler feedwater,
(c) plant for degassing boiler feedwater, comprising a feedwater vessel having a heat exchanger present therein for heat exchange between synthesis gas and the boiler feedwater and having at least one dome which is installed on the feedwater vessel and has internals for gas-liquid mass transfer, for example beds of random packing elements or structured packings, via which dome the boiler feedwater and/or the condensate separated off from the synthesis gas can be introduced into the feedwater vessel,
(d) heat exchanger for heat exchange of the synthesis gas with the surrounding air,
(e) condensate separator for separating condensate from the synthesis gas,
(f) a pipe for feeding the boiler feedwater from the boiler feedwater production which is not part of the plant to the degassing plant (c), with the pipe being laid in such a way that it opens into the dome which serves to supply the boiler feedwater to be degassed to the feedwater vessel of the degassing plant,
(g) pipe for transfer of the condensate from the condensate separator (e) to the degassing plant (c), with the pipe being laid in such a way that it opens into the dome which serves to supply the condensate to the feedwater vessel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201880038050.5A CN110719890B (en) | 2017-06-20 | 2018-06-06 | Method and apparatus for cooling syngas |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP17400040.6A EP3418253B1 (en) | 2017-06-20 | 2017-06-20 | Method for the cooling of synthesis gas |
| EP17400040.6 | 2017-06-20 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| WO2018233872A1 true WO2018233872A1 (en) | 2018-12-27 |
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| PCT/EP2018/025146 WO2018233872A1 (en) | 2017-06-20 | 2018-06-06 | Process and plant for cooling synthesis gas |
Country Status (3)
| Country | Link |
|---|---|
| EP (1) | EP3418253B1 (en) |
| CN (1) | CN110719890B (en) |
| WO (1) | WO2018233872A1 (en) |
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| WO2012031683A1 (en) * | 2010-09-10 | 2012-03-15 | Uhde Gmbh | Method and device for producing process vapor and boiler feed steam in a heatable reforming reactor for producing synthesis gas |
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| WO2017008915A1 (en) * | 2015-07-10 | 2017-01-19 | L'air Liquide Societe Anonyme Pour L'etude Et Exploitation Des Procedes Georges Claude | Process and plant for cooling synthesis gas |
| EP3124433A1 (en) * | 2015-07-27 | 2017-02-01 | L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Installation and method for cooling synthesis gas |
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| GB1538425A (en) * | 1975-03-03 | 1979-01-17 | Ici Ltd | Steam-hydrocarbon process |
| EP2233430A1 (en) * | 2009-03-24 | 2010-09-29 | Hydrogen Energy International Limited | Process for generating hydrogen and carbon dioxide |
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2017
- 2017-06-20 EP EP17400040.6A patent/EP3418253B1/en active Active
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2018
- 2018-06-06 WO PCT/EP2018/025146 patent/WO2018233872A1/en active Application Filing
- 2018-06-06 CN CN201880038050.5A patent/CN110719890B/en active Active
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| DE1950055A1 (en) | 1969-10-03 | 1971-04-15 | Moco Industrieanlagen H Scholz | Pneumatic conveyor system with the delivery of the material to be conveyed into a pressure vessel arranged in the main line |
| DE102004030246A1 (en) * | 2004-06-23 | 2006-01-12 | Caloric Anlagenbau Gmbh | Producing hydrogen by steam reforming comprises preheating boiler feed water going to a deaerator by heat exchange with the water leaving the deaerator |
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Also Published As
| Publication number | Publication date |
|---|---|
| EP3418253B1 (en) | 2020-11-25 |
| CN110719890A (en) | 2020-01-21 |
| EP3418253A1 (en) | 2018-12-26 |
| CN110719890B (en) | 2023-04-04 |
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