CN112624044B - Reactor for producing superheated steam by CO conversion with adiabatic serial isothermal and gas conversion process - Google Patents
Reactor for producing superheated steam by CO conversion with adiabatic serial isothermal and gas conversion process Download PDFInfo
- Publication number
- CN112624044B CN112624044B CN202110001584.4A CN202110001584A CN112624044B CN 112624044 B CN112624044 B CN 112624044B CN 202110001584 A CN202110001584 A CN 202110001584A CN 112624044 B CN112624044 B CN 112624044B
- Authority
- CN
- China
- Prior art keywords
- gas
- shell
- axial
- heat exchange
- reaction section
- 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.)
- Active
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract 47
- 238000000034 method Methods 0.000 title claims abstract 5
- 229920006395 saturated elastomer Polymers 0.000 claims abstract 5
- 239000003507 refrigerant Substances 0.000 claims 12
- 230000035939 shock Effects 0.000 claims 9
- 239000002994 raw material Substances 0.000 claims 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 5
- 238000010521 absorption reaction Methods 0.000 claims 1
- 230000008020 evaporation Effects 0.000 claims 1
- 238000001704 evaporation Methods 0.000 claims 1
- 238000005192 partition Methods 0.000 abstract 2
- 230000009286 beneficial effect Effects 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 238000013021 overheating Methods 0.000 abstract 1
Classifications
-
- 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
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/14—Handling of heat and steam
-
- 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
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
-
- 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
Landscapes
- 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)
- Physical Or Chemical Processes And Apparatus (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The application discloses a reactor for producing superheated steam by CO conversion with adiabatic serial isothermal, which comprises a shell and a partition plate seal head, wherein the partition plate seal head divides the shell into a radial shell and an axial shell; a centrifugal radial reaction section is arranged in the radial shell, and an axial reaction section is arranged in the axial shell; a heat exchange cylinder and a U-shaped heat exchange tube group arranged in the heat exchange cylinder are arranged in the axial shell; the centrifugal radial reaction section is provided with a central gas distribution pipe communicated with the heat exchange cylinder, an outer gas cylinder is sleeved outside the central gas distribution pipe, and a heat transfer tube array is arranged between the central gas distribution pipe and the outer gas cylinder; the feed gas can generate primary shift gas in the axial reaction section; and then generating secondary conversion gas in the centrifugal radial reaction section. The application also discloses a gas shift process adopting the reactor. The application can realize the functions of adiabatic reaction, temperature control reaction, saturated steam production, steam overheating and the like, and is beneficial to the on-site equipment arrangement conciseness, pipeline saving and investment saving.
Description
Technical Field
The invention relates to a reactor for producing superheated steam by CO conversion with adiabatic serial isothermal and a gas conversion process.
Background
Because of the presence of certain amounts of COS in the feed gas, these COS are converted to H 2 S during the CO shift reaction, which can cause corrosion to equipment and poisoning of the catalyst. In addition, a certain amount of dust and other harmful substances are inevitably present in the raw gas, and even if the raw gas is subjected to detoxification and purification treatment before the shift reaction, the removal effect of the dust and other harmful substances is limited in practice due to the limitation of temperature during the detoxification and purification treatment, and the dust can block the catalyst passage after entering the shift reactor, thereby affecting the catalytic effect of the catalyst. In addition, in the existing equipment, after hot water generated by heat exchange enters a steam drum, corresponding steam is produced, and if the steam is required to be superheated, the steam is required to be heated for a second time through other heating devices, so that the arrangement quantity of the equipment is increased.
Disclosure of Invention
In order to solve the problems, the invention firstly provides a reactor for producing superheated steam through heat-insulating serial isothermal CO conversion, which comprises a shell extending along the vertical direction, wherein a baffle head is arranged in the shell, and the baffle head divides the shell into a radial shell positioned at the upper side and an axial shell positioned at the lower side;
a centrifugal radial reaction section is arranged in the radial shell, and an axial reaction section is arranged in the axial shell;
A heat exchange cylinder is axially arranged at the center of the axial shell, and the heat exchange cylinder is provided with an airflow channel; a U-shaped heat exchange tube group is arranged in the heat exchange tube, both ends of the U-shaped heat exchange tube group are communicated with the outside of the shell and respectively communicated with a steam inlet tube and a steam outlet tube, and the U-shaped heat exchange tube group is used for generating superheated steam;
The centrifugal radial reaction section is provided with a central gas distribution pipe which is downwards communicated with the heat exchange cylinder, the top of the radial shell is provided with a conversion gas outlet, and the axial shell is provided with a raw gas inlet;
An outer air cylinder is sleeved outside the central air distribution pipe, a heat transfer tube array extending in the vertical direction is arranged between the central air distribution pipe and the outer air cylinder, the lower end of the heat transfer tube array is connected with a refrigerant inlet pipe, and the refrigerant inlet pipe downwards penetrates through the baffle head and the axial reaction section and then extends out of the bottom of the shell to form a refrigerant inlet;
An annular gap is formed between the outer air cylinder and the shell, and the annular gap is communicated with the conversion air outlet;
the upper end of the heat transfer tube array is connected with a refrigerant outlet pipe which extends upwards from the fixed part of the shell and is formed into a refrigerant outlet; the central air distribution pipe is provided with an air distribution hole, the outer air cylinder is provided with an exhaust hole, the air distribution hole and the exhaust hole are through holes, and the air distribution hole and the exhaust hole are arranged according to the prior art;
The raw material gas can enter the axial shell through the raw material gas inlet and is subjected to primary conversion in the axial reaction section to generate primary conversion gas; the primary conversion gas can enter the heat exchange tube through the gas flow channel, then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion, secondary conversion gas is generated, and the secondary conversion gas is discharged from the conversion gas outlet.
In the application, in order to ensure the strength of the shell, the radial shell is made of 14CrMoR materials, and the axial shell including the lower seal head is made of 14CrMoR+S32168 composite material plates, wherein the S32168 material layer is positioned on the inner side. After the S32168 stainless steel material is lined in the axial shell, the corrosion resistance of the shell at high temperature can be improved, and the service life of the equipment is ensured.
In the application, the shell comprises a straight cylinder, an upper end socket and a lower end socket, wherein the upper end socket and the straight cylinder are detachably connected together, and an omega seal is arranged between the upper end socket and the straight cylinder in a pad mode. The upper seal head is detachably arranged at the top of the straight cylinder, and the inside of the equipment can be installed and overhauled through the upper end of the straight cylinder. Omega seals are employed to ensure the tightness of the device at high temperatures and pressures.
According to the application, the raw material gas is subjected to preliminary reaction in the axial reaction section, the temperature in the axial reaction section can be set in a temperature range which is favorable for converting COS into H 2 S, other organic matters in the raw material gas are converted to the greatest extent, the organic matters are prevented from entering the centrifugal radial reaction section, and the centrifugal radial reaction section is ensured to run for a long time. Because the axial reaction section has the advantage of replacing the catalyst, when the reaction temperature of the axial reaction section is set in a higher range, products generated by the reaction of the gas organic matters are favorable to be kept in the axial reaction section, and in addition, toxic substances, dust and other impurities in the raw material gas are also kept in the axial reaction section, so that the catalyst in the centrifugal radial reaction section is required to be replaced after the catalyst in the axial reaction section is replaced for a plurality of times in the production process.
The steam can be superheated by utilizing the high reaction temperature of the axial reaction section to improve the grade of the steam, so that the produced superheated steam can be directly used as power steam.
The application can realize the functions of adiabatic reaction, temperature control reaction, saturated steam production, steam overheating and the like as a composite tower. Under the condition of being favorable for realizing the technological process requirements, the on-site equipment arrangement is simple, the pipelines are saved, and the investment is saved.
Further, a heat exchanger mounting port for the U-shaped heat exchange tube group to enter and exit is arranged at the bottom of the shell, the lower end of the heat exchange tube is open and is formed into a heat exchanger inlet and outlet, the heat exchanger mounting port is opposite to the heat exchanger inlet and outlet, and the U-shaped heat exchange tube group can freely enter and exit the heat exchange tube through the heat exchanger mounting port and the heat exchanger inlet and outlet. When the U-shaped heat exchange tube group needs to be replaced, the U-shaped heat exchange tube group can be extracted through the heat exchanger mounting port and the heat exchanger inlet and outlet, and then a new U-shaped heat exchange tube group is replaced. The design ensures that the U-shaped heat exchange tube group has higher convenience in replacement, and the U-shaped heat exchange tube group can be replaced without entering the shell.
Further, in order to sufficiently absorb the reaction heat in the axial reaction section, a distance is provided between the lower end of the heat exchange tube and the inner surface of the bottom of the housing, the distance being formed as an air flow passage. Because the air flow channel is arranged at the lower end of the heat exchange tube, primary heat exchange air can be contacted with the U-shaped heat exchange tube group to the greatest extent and exchanges heat in the process of flowing through the heat exchange tube, and the heat exchange efficiency can be effectively improved.
Further, the central gas distribution pipe extends upwards out of the top of the shell to form a raw gas near-route inlet. The raw material near-line inlet can be used as a cold shock gas inlet of the centrifugal radial reaction section. In traditional equipment, generally set up cold shock gas pipe alone, cold shock gas gets into equipment back, directly gets into the reaction bed layer, reduces reaction temperature, but because cold shock gas can't in time to the central region diffusion of bed layer, cause in the reaction bed layer, the reaction temperature in local region can't effectively reduce. In the application, the central gas distribution pipe is used as the cold shock pipe at the same time, and after entering the reactor, the cold shock gas is firstly mixed with primary conversion gas from the axial reaction section, and the temperature of the primary conversion gas is directly reduced, so that the reaction is more stable, and the problem of local reaction overheating can be effectively eliminated. After the design is adopted, the difference of the reaction temperature in the centrifugal radial reaction section can be reduced from the current 50-80 ℃ to 10-20 ℃.
Further, in order to facilitate effective control of the reaction temperature of the axial reaction section, two axial beds are arranged in the axial reaction section, the two axial beds are arranged at intervals along the vertical direction, and the raw material gas inlet is arranged at the upper side of the axial bed on the upper layer; a cold shock gas inlet pipe is arranged between the two axial beds. A catalyst discharge pipe is arranged corresponding to each axial bed layer so as to discharge the catalyst in each axial bed layer.
Further, the heat transfer tubes are divided into at least three groups, each group of heat transfer tubes is provided with a refrigerant inlet tube, and the refrigerant inlet tubes are uniformly arranged around the heat exchange tube;
A cold shock gas distribution pipe is arranged between the two axial beds, the cold shock gas distribution pipe is annular, the cold shock gas distribution pipe comprises an annular pipe sleeved on a refrigerant inlet pipe and a connecting pipe connected between two adjacent annular pipes, and the cold shock gas inlet pipe is connected to the cold shock gas distribution pipe; cold shock air holes are arranged on the cold shock air distribution pipe. And cold shock holes are formed in the annular pipe and the connecting pipe.
The second cold shock gas enters the cold shock gas distribution pipe from the cold shock gas holes and then enters the two axial beds, in order to make the cold shock gas uniformly enter the two axial beds, the cold shock gas holes are formed in the annular pipe and the connecting pipe, and the cold shock gas holes are formed in the upper side and the lower side of the annular pipe and the connecting pipe.
In order to ensure uniform distribution of the second cold shock gas, the refrigerant inlet pipe is sleeved with the annular pipe, so that the cold shock gas distribution pipe is furthest arranged at the optimal position, and the second cold shock gas can be uniformly distributed.
Further, the refrigerant inlet is connected to a hot water outlet pipe of a drum, the refrigerant outlet is connected to a hot water inlet pipe of the drum, and a steam discharge pipe of the drum is communicated with a steam inlet. The design can lead the reactor to continuously heat the same water source, firstly, the centrifugal radial reaction section heats soft water in the steam drum to generate saturated water, and then the axial reaction section superheats saturated steam flashed by the steam drum to produce superheated steam so as to fully utilize reaction heat and achieve the aim of producing superheated steam.
As the saturated water and the superheated steam are produced aiming at the same steam drum, the arrangement of related pipelines can be effectively reduced, and the investment is saved.
Secondly, the application also provides a gas shift process, which adopts the reactor of any one of the above steps, and comprises the following steps:
The raw material gas enters the axial shell through the raw material gas inlet and is subjected to primary conversion in the axial reaction section to generate primary conversion gas; the primary conversion gas can enter the heat exchange cylinder through the gas flow channel, then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion, secondary conversion gas is generated, and the secondary conversion gas is discharged from the conversion gas outlet; the reaction temperature in the axial reaction section is higher than that in the centrifugal radial reaction section;
Saturated water of the steam drum enters the heat transfer tube array through the refrigerant inlet, and superheated water is formed after heat exchange of the absorption centrifugal radial reaction section, is discharged from the refrigerant outlet and returns to the steam drum; the superheated water in the steam drum is subjected to flash evaporation to obtain saturated steam, and the saturated steam enters the heat exchange tube through the steam inlet to absorb the heat converted from the axial reaction section, so that the saturated steam becomes superheated steam.
In the conversion process, the raw material gas is subjected to preliminary reaction in the axial reaction section, the temperature in the axial reaction section can be set in a temperature range which is favorable for converting COS into H 2 S, other organic matters in the raw material gas are converted to the greatest extent, the organic matters are prevented from entering the centrifugal radial reaction section, and the centrifugal radial reaction section is ensured to be capable of running for a long time. Because the axial reaction section has the advantage of replacing the catalyst, when the reaction temperature of the axial reaction section is set in a higher range, products generated by the reaction of the gas organic matters are favorable to be kept in the axial reaction section, and in addition, toxic substances, dust and other impurities in the raw material gas are also kept in the axial reaction section, so that the catalyst in the centrifugal radial reaction section is required to be replaced after the catalyst in the axial reaction section is replaced for a plurality of times in the production process.
The steam can be superheated by utilizing the high reaction temperature of the axial reaction section to improve the grade of the steam, so that the produced superheated steam can be directly used as power steam.
Further, the first cold shock gas enters the central gas distribution pipe from the raw gas near-route inlet at the top of the shell, and the temperature in the centrifugal radial reaction section is adjusted. The second cold shock gas enters the axial reaction section through the cold shock gas inlet pipe, and the temperature in the axial reaction section is adjusted.
In the application, the central gas distribution pipe is used as the cold shock pipe at the same time, and after entering the reactor, the cold shock gas is firstly mixed with primary conversion gas from the axial reaction section, and the temperature of the primary conversion gas is directly reduced, so that the reaction is more stable, and the problem of local reaction overheating can be effectively eliminated. After the design is adopted, the difference of the reaction temperature in the centrifugal radial reaction section can be reduced from the current 50-80 ℃ to 10-20 ℃.
Specifically, the reaction temperature of the axial reaction section is 390-410 ℃, and the reaction temperature of the centrifugal radial reaction section is 280-295 ℃. In the gas shift process, the temperature of saturated steam entering the heat exchange tube is 245-255 ℃, and the temperature of superheated steam discharged from the heat exchange tube is 395-405 ℃.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present invention.
Detailed Description
Referring to fig. 1, a reactor for producing superheated steam by CO conversion with adiabatic serial isothermal includes a housing 10 extending in a vertical direction, wherein the housing 10 specifically includes a straight cylinder 11, an upper end enclosure 12 located at the top of the straight cylinder, and a lower end enclosure 13 located at the bottom of the straight cylinder. The upper end enclosure 12 and the straight cylinder 11 are detachably connected together through bolts, an omega seal is arranged between the upper end enclosure and the straight cylinder in a pad mode, and the lower end enclosure is directly welded on the straight cylinder.
A bulkhead seal 14 is provided in the housing, and the bulkhead seal 14 is welded to the inner wall of the straight tube 11, and divides the housing 10 into a radial housing located on the upper side and an axial housing located on the lower side.
A centrifugal radial reaction section 101 is provided in the radial housing, and an axial reaction section 102 is provided in the axial housing.
A heat exchange tube 71 is provided in the axial direction in the center of the axial housing, and a U-shaped heat exchange tube group 61 is installed in the heat exchange tube 71. A bottom hole is formed in the bottom of the lower seal head 13, a flange 17 is welded on the bottom hole, a heat exchange tube plate 63 is mounted on the lower side of the flange 17 in a sealing mode through bolts, and the heat exchange seal head 62 is welded on the lower side of the heat exchange tube plate 63. A dividing plate 64 is welded in the heat exchange end enclosure 62 and is positioned in the heat exchange end enclosure 62 and welded between the heat exchange end enclosure and the heat exchange tube plate, an inner cavity between the heat exchange end enclosure and the heat exchange tube plate is divided into an inlet cavity and an outlet cavity, a steam inlet pipe 65 is welded on the heat exchange end enclosure and communicated with the inlet cavity, and a steam outlet pipe 66 is welded on the heat exchange end enclosure and communicated with the outlet cavity.
Both ends of the U-shaped tube of the U-shaped heat exchange tube group 61 are welded on the heat exchange tube plate and are respectively communicated with the inlet cavity and the outlet cavity. The central hole of the flange 17 is formed as a heat exchanger mounting port into and out of the U-shaped heat exchange tube group.
The lower end of the heat exchange tube is open and is formed into a heat exchanger inlet and a heat exchanger outlet, and the heat exchanger inlet and the heat exchanger outlet are opposite to the heat exchanger mounting port. A distance 72 is provided between the lower end of the heat exchange tube and the inner surface of the bottom of the housing, which distance 72 forms an air flow channel.
When the U-shaped heat exchange tube group 61 needs to be replaced, the bolts of the connecting flange 17 and the heat exchange tube plate 63 are detached, then the U-shaped heat exchange tube group 61, the heat exchange tube plate 63 and the heat exchange seal head 62 are integrally detached, the U-shaped heat exchange tube group 61, the heat exchange tube plate 63 and the heat exchange seal head 62 are extracted from the shell through the central hole of the flange 17 and the inlet and the outlet of the heat exchanger, and then a new U-shaped heat exchange tube group 61, the heat exchange tube plate 63 and the heat exchange seal head 62 are replaced. Namely, the U-shaped heat exchange tube group can freely enter and exit the heat exchange tube through the heat exchanger mounting port and the heat exchanger inlet and outlet.
The centrifugal radial reaction section 101 has a central gas distribution pipe 31, the central gas distribution pipe 31 and the heat exchange tube 71 are coaxially arranged and connected together, and the central gas distribution pipe 31 is downwardly communicated with the heat exchange tube 71.
The outer air cylinder 32 is sleeved outside the central air distribution pipe, four heat transfer pipe groups 20 are arranged between the central air distribution pipe and the outer air cylinder, each heat transfer pipe group 20 comprises a plurality of heat transfer pipes 21 extending along the vertical direction, an upper pipe plate 44 and a lower pipe plate 43 are arranged corresponding to each heat transfer pipe group 20, and two ends of each heat transfer pipe group 21 are welded to the upper pipe plate 44 and the lower pipe plate 43 respectively. An upper inner seal 45 is arranged on the upper side of the upper tube plate 44, a refrigerant outlet pipe 46 is arranged on the upper inner seal, and the refrigerant outlet pipe 46 extends upwards out of the upper seal to form a refrigerant outlet 461. The central air distribution pipe is provided with air distribution holes, the outer air cylinder is provided with air exhaust holes, the air distribution holes and the air exhaust holes are shown in the drawings, and the prior art can be adopted specifically.
A lower inner seal head 42 is arranged at the lower side of the lower tube plate 43, a refrigerant inlet pipe 41 is arranged on the lower inner seal head, and the refrigerant inlet pipe 41 downwards penetrates through the baffle seal head and the axial reaction section, extends out of the lower seal head and is formed into a refrigerant inlet 411. The refrigerant inlet pipes 41 are uniformly arranged around the heat exchange tube 71.
Two axial beds are provided in the axial reaction section, a first axial bed 51 and a second axial bed 56, respectively, the first axial bed 51 being located on the upper side of the second axial bed 56. A catalyst support plate 52 and a catalyst gland 53 are provided corresponding to each axial bed. The feed gas inlet 15 is arranged on the upper side of the first axial bed 51, i.e. the feed gas inlet is arranged on the upper side of the upper axial bed.
A catalyst discharge pipe 54 is provided corresponding to each axial bed.
The two axial beds are arranged at intervals in the vertical direction, and a cold shock gas inlet pipe 58 is arranged between the two axial beds.
A cold shock gas distribution pipe is arranged between the two axial beds, the cold shock gas distribution pipe is annular, the cold shock gas distribution pipe comprises an annular pipe 581 sleeved on a refrigerant inlet pipe and a connecting pipe 582 connected between two adjacent annular pipes, and the cold shock gas inlet pipe 58 is connected to the cold shock gas distribution pipe; the cold shock gas distribution pipe is provided with cold shock gas holes, and in the embodiment, the annular pipe and the connecting pipe are provided with cold shock gas holes.
The upper seal head is provided with a conversion gas outlet 16, and an annular space is formed between the outer air cylinder and the outer shell, and the annular space is communicated with the conversion gas outlet.
The central gas distribution pipe 31 extends upwards to form a raw gas near-path inlet 313 after extending upwards from the upper end enclosure.
The raw material gas can enter the axial shell through the raw material gas inlet 15 and is subjected to primary conversion in the axial reaction section to generate primary conversion gas; the primary conversion gas can enter the heat exchange tube through the gas flow channel, then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion, secondary conversion gas is generated, and the secondary conversion gas is discharged from the conversion gas outlet. The first cold shock gas enters the central gas distribution pipe 31 from the raw gas near-line inlet 313, then reacts in the centrifugal radial reaction section, and the reaction temperature in the centrifugal radial reaction section is adjusted. The second cold shock gas enters the axial reaction section from the cold shock gas inlet pipe 58 to participate in the reaction, and the reaction temperature of the axial reaction section is adjusted.
In this embodiment, the refrigerant inlet 411 is connected to the hot water outlet pipe 81 of a drum 80, the refrigerant outlet 461 is connected to the hot water inlet pipe 82 of the drum, the steam outlet pipe 83 of the drum is connected to the steam inlet 83, and the soft water replenishment pipe 84 is installed on the drum 80.
The following describes a gas shift process using the reactor described above, comprising the steps of:
The raw material gas enters the axial shell through the raw material gas inlet and is subjected to primary conversion in the axial reaction section to generate primary conversion gas; the primary conversion gas can enter the heat exchange cylinder through the gas flow channel, then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion, secondary conversion gas is generated, and the secondary conversion gas is discharged from the conversion gas outlet; the reaction temperature in the axial reaction section is higher than that in the centrifugal radial reaction section.
Saturated water of the steam drum enters the heat transfer tube array through the refrigerant inlet, and superheated water is formed after heat exchange of the absorption centrifugal radial reaction section, is discharged from the refrigerant outlet and returns to the steam drum; the superheated water in the steam drum is subjected to flash evaporation to obtain saturated steam, and the saturated steam enters the heat exchange tube through the steam inlet to absorb the heat converted from the axial reaction section, so that the saturated steam becomes superheated steam.
The first cold shock gas enters the central gas distribution pipe from a raw gas close-route inlet at the top of the shell, and the reaction temperature in the centrifugal radial reaction section is adjusted. The second cold shock gas enters the axial reaction section through the cold shock gas inlet pipe, and the reaction temperature in the axial reaction section is adjusted.
In this example, the reaction temperature in the axial reaction zone is 395-405℃and in the centrifugal radial reaction zone is 285-290 ℃. The saturated steam flashed from the drum 80 is formed into superheated steam having a temperature of 400 c through the U-shaped heat exchange tube set, and the saturated steam inlet temperature is 250 c.
Claims (10)
1. A reactor for producing superheated steam by CO conversion with adiabatic serial isothermal is characterized in that,
The device comprises a shell extending along the vertical direction, wherein a baffle head is arranged in the shell and divides the shell into a radial shell positioned at the upper side and an axial shell positioned at the lower side;
a centrifugal radial reaction section is arranged in the radial shell, and an axial reaction section is arranged in the axial shell;
A heat exchange cylinder is axially arranged at the center of the axial shell, and the heat exchange cylinder is provided with an airflow channel; a U-shaped heat exchange tube group is arranged in the heat exchange tube, both ends of the U-shaped heat exchange tube group are communicated with the outside of the shell and respectively communicated with a steam inlet tube and a steam outlet tube, and the U-shaped heat exchange tube group is used for generating superheated steam;
The centrifugal radial reaction section is provided with a central gas distribution pipe which is downwards communicated with the heat exchange cylinder, the top of the radial shell is provided with a conversion gas outlet, and the axial shell is provided with a raw gas inlet;
An outer air cylinder is sleeved outside the central air distribution pipe, a heat transfer tube array extending in the vertical direction is arranged between the central air distribution pipe and the outer air cylinder, the lower end of the heat transfer tube array is connected with a refrigerant inlet pipe, and the refrigerant inlet pipe downwards penetrates through the baffle head and the axial reaction section and then extends out of the bottom of the shell to form a refrigerant inlet;
An annular gap is formed between the outer air cylinder and the shell, and the annular gap is communicated with the conversion air outlet;
The upper end of the heat transfer tube array is connected with a refrigerant outlet pipe which extends upwards from the fixed part of the shell and is formed into a refrigerant outlet;
The raw material gas can enter the axial shell through the raw material gas inlet and is subjected to primary conversion in the axial reaction section to generate primary conversion gas; the primary conversion gas can enter the heat exchange tube through the gas flow channel, then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion, secondary conversion gas is generated, and the secondary conversion gas is discharged from the conversion gas outlet.
2. A reactor according to claim 1,
The bottom of the shell is provided with a heat exchanger mounting port for the U-shaped heat exchange tube group to enter and exit, the lower end of the heat exchange tube is open and is formed into a heat exchanger inlet and outlet, the heat exchanger mounting port is opposite to the heat exchanger inlet and outlet, and the U-shaped heat exchange tube group can freely enter and exit the heat exchange tube through the heat exchanger mounting port and the heat exchanger inlet and outlet.
3. A reactor according to claim 2, wherein,
The lower end of the heat exchange tube is spaced from the inner surface of the bottom of the housing by a distance which forms an air flow passage.
4. A reactor according to claim 1,
The central gas distribution pipe extends upwards out of the top of the shell to form a raw gas near-route inlet.
5. A reactor according to claim 1,
Two axial beds are arranged at the axial reaction section and are arranged at intervals along the vertical direction, and the raw material gas inlet is arranged at the upper side of the axial bed at the upper layer; a cold shock gas inlet pipe is arranged between the two axial beds.
6. A reactor according to claim 5, wherein,
The heat transfer tubes are divided into at least three groups, each group of heat transfer tubes is provided with a refrigerant inlet tube, and the refrigerant inlet tubes are uniformly distributed around the heat exchange tube;
A cold shock gas distribution pipe is arranged between the two axial beds, the cold shock gas distribution pipe is annular, the cold shock gas distribution pipe comprises an annular pipe sleeved on a refrigerant inlet pipe and a connecting pipe connected between two adjacent annular pipes, and the cold shock gas inlet pipe is connected to the cold shock gas distribution pipe; cold shock air holes are arranged on the cold shock air distribution pipe.
7. A reactor according to claim 1,
The refrigerant inlet is connected to a hot water outlet pipe of a steam drum, the refrigerant outlet is connected to a hot water inlet pipe of the steam drum, and a steam discharge pipe of the steam drum is communicated with a steam inlet.
8. A gas shift process employing the reactor of any one of claims 1-7, comprising the steps of:
The raw material gas enters the axial shell through the raw material gas inlet and is subjected to primary conversion in the axial reaction section to generate primary conversion gas; the primary conversion gas can enter the heat exchange cylinder through the gas flow channel, then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion, secondary conversion gas is generated, and the secondary conversion gas is discharged from the conversion gas outlet; the reaction temperature in the axial reaction section is higher than that in the centrifugal radial reaction section;
Saturated water of the steam drum enters the heat transfer tube array through the refrigerant inlet, and superheated water is formed after heat exchange of the absorption centrifugal radial reaction section, is discharged from the refrigerant outlet and returns to the steam drum; the superheated water in the steam drum is subjected to flash evaporation to obtain saturated steam, and the saturated steam enters the heat exchange tube through the steam inlet to absorb the heat converted from the axial reaction section, so that the saturated steam becomes superheated steam.
9. A gas shift process as defined in claim 8, wherein,
The first cold shock gas enters the central gas distribution pipe from a raw gas close-route inlet at the top of the shell, and the temperature in the centrifugal radial reaction section is adjusted.
10. A gas shift process as claimed in claim 8 or 9, characterized in that,
The reaction temperature of the axial reaction section is 390-410 ℃, and the reaction temperature of the centrifugal radial reaction section is 280-295 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110001584.4A CN112624044B (en) | 2021-01-04 | 2021-01-04 | Reactor for producing superheated steam by CO conversion with adiabatic serial isothermal and gas conversion process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110001584.4A CN112624044B (en) | 2021-01-04 | 2021-01-04 | Reactor for producing superheated steam by CO conversion with adiabatic serial isothermal and gas conversion process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112624044A CN112624044A (en) | 2021-04-09 |
| CN112624044B true CN112624044B (en) | 2024-07-12 |
Family
ID=75291436
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110001584.4A Active CN112624044B (en) | 2021-01-04 | 2021-01-04 | Reactor for producing superheated steam by CO conversion with adiabatic serial isothermal and gas conversion process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112624044B (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN214399816U (en) * | 2021-01-04 | 2021-10-15 | 南京聚拓化工科技有限公司 | Heat-insulation-series isothermal reactor capable of generating superheated steam during CO conversion |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002224570A (en) * | 2001-02-05 | 2002-08-13 | Toyota Central Res & Dev Lab Inc | Catalyst for CO shift reaction |
| JP4015391B2 (en) * | 2001-09-07 | 2007-11-28 | 三菱重工業株式会社 | CO shift catalyst and method for producing the same |
| CN203075923U (en) * | 2012-11-16 | 2013-07-24 | 航天长征化学工程股份有限公司 | Axial-radial constant-temperature conversion reactor |
| CN104069777B (en) * | 2014-07-14 | 2015-12-16 | 南京博扬化工科技有限公司 | A kind of isothermal adiabatic radial compound formula reactor |
| CN203944361U (en) * | 2014-07-14 | 2014-11-19 | 南京博扬化工科技有限公司 | The adiabatic radial compound formula of a kind of isothermal reactor |
| CN105032497B (en) * | 2015-07-13 | 2017-06-13 | 福州大学化肥催化剂国家工程研究中心 | Carbon monoxide transformation catalyst carrier, the catalyst based on carrier and preparation method |
| CN208389981U (en) * | 2018-04-09 | 2019-01-18 | 南京聚拓化工科技有限公司 | The radial methanol reactor of combined type heat exchange |
| CN111729619B (en) * | 2020-06-28 | 2023-12-19 | 南京聚拓化工科技有限公司 | Multistage composite conversion device and conversion process |
| CN111732075B (en) * | 2020-06-28 | 2023-06-27 | 南京聚拓化工科技有限公司 | Composite heat-insulating serial temperature-control shift converter device and shift process |
-
2021
- 2021-01-04 CN CN202110001584.4A patent/CN112624044B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN214399816U (en) * | 2021-01-04 | 2021-10-15 | 南京聚拓化工科技有限公司 | Heat-insulation-series isothermal reactor capable of generating superheated steam during CO conversion |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112624044A (en) | 2021-04-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102887480B (en) | CO shift technique by connecting isothermal shift and thermal insulation shift in series | |
| SU1056878A3 (en) | Converter for methane production | |
| CN210915299U (en) | Hydrogen production machine | |
| CN108404821B (en) | Energy-saving efficient radial methanol reactor | |
| RU148799U1 (en) | HEAT EXCHANGE REACTOR | |
| RU2185879C2 (en) | Plant for performing endothermic and exothermic reactions and reforming unit | |
| CN106964301B (en) | Novel furnace type reactor with built-in raw material preheating and steam superheating device | |
| CN214399816U (en) | Heat-insulation-series isothermal reactor capable of generating superheated steam during CO conversion | |
| CN112624044B (en) | Reactor for producing superheated steam by CO conversion with adiabatic serial isothermal and gas conversion process | |
| CN202516536U (en) | Shift-converter with built-in cold wall | |
| CN102886231B (en) | Fully-radial isothermal CO (carbon monoxide) conversion furnace | |
| CN220206451U (en) | Combined synthetic ammonia heat recovery equipment with steam superheater | |
| CN108970548B (en) | Isothermal shift reaction device | |
| CN215655077U (en) | Ring box type water heat transfer temperature control reactor | |
| CN108421505B (en) | Radial-axial combined reactor suitable for strong exothermic reaction | |
| CN110898769B (en) | Poly-generation isothermal transformation process matched with pulverized coal gasification process and isothermal transformation furnace | |
| CN221452551U (en) | Constant temperature type methanol synthesis tower | |
| CN110921617B (en) | Isothermal transformation parallel air-cooled transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace | |
| CN110921620B (en) | Isothermal transformation parallel adiabatic transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace | |
| CN110921621B (en) | Low-steam-ratio poly-generation isothermal transformation process and isothermal transformation furnace matched with pulverized coal gasification | |
| CN110305698B (en) | A heat extraction system and a gasification reactor equipped with the heat extraction system | |
| CN220990739U (en) | Temperature-control shift reaction furnace with double-ball structure | |
| CN110921618B (en) | Air-cooled transformation series isothermal transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace | |
| CN110803681B (en) | Gas-cooled transformation series isothermal transformation hydrogen production process matched with coal water slurry gasification and isothermal transformation furnace | |
| CN210801133U (en) | Regular blowdown expander |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |