CN112624044A - Heat-insulation serial isothermal CO conversion reactor capable of producing superheated steam and coal gas conversion process - Google Patents
Heat-insulation serial isothermal CO conversion reactor capable of producing superheated steam and coal gas conversion process Download PDFInfo
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- 206010024769 Local reaction Diseases 0.000 description 2
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- 239000012535 impurity Substances 0.000 description 2
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- 239000005416 organic matter Substances 0.000 description 2
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- 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
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Abstract
The invention discloses a reactor for CO conversion with heat insulation and isothermal series and simultaneously producing superheated steam, which comprises a shell and a partition plate end socket, wherein the shell is divided into a radial shell and an axial shell by the partition plate end socket; 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 installed in the heat exchange cylinder are arranged in the axial shell; the centrifugal radial reaction section is provided with a central air distribution pipe communicated with the heat exchange cylinder, an outer air cylinder is sleeved outside the central air distribution pipe, and a heat transfer array pipe is arranged between the central air distribution pipe and the outer air cylinder; the feed gas can generate primary conversion gas in the axial reaction section; secondary shift gas is then generated in the centrifugal radial reaction zone. The application also discloses a coal gas shift process adopting the reactor. The system can realize functions of adiabatic reaction, temperature control reaction, saturated steam production, steam overheating and the like, and is beneficial to concise field equipment arrangement, pipeline saving and investment saving.
Description
Technical Field
The invention relates to a reactor for CO conversion with adiabatic series isothermy and producing superheated steam and a coal gas conversion process.
Background
Due to the presence of a certain amount of COS in the feed gas, these COS are converted into H during the CO shift reaction2S, not only causes corrosion to equipment, but also causes catalysisPoisoning of the agent. In addition, a certain amount of dust and other harmful substances inevitably exist in the feed gas, even if the feed gas is subjected to detoxification and purification treatment before the shift reaction, due to the temperature limitation in the detoxification and purification treatment process, the removal effect on the dust and other harmful substances is limited in practice, and the dust in the feed gas can block the channel of the catalyst after entering the shift reactor, so that the catalytic effect of the catalyst is influenced. In addition, in the existing equipment, after hot water generated by heat exchange enters a steam drum, corresponding steam is generated, and if the steam needs to become superheated steam, the superheated steam needs to be secondarily heated by other heating devices, so that the arrangement number of the equipment is increased.
Disclosure of Invention
In order to solve the problems, the invention firstly provides a heat-insulation serial isothermal reactor for CO conversion and superheated steam generation, which comprises a shell extending along the vertical direction, wherein a partition plate end socket 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 arranged at the central part of the axial shell along the axial direction, and the heat exchange cylinder is provided with an airflow channel; a U-shaped heat exchange tube group is arranged in the heat exchange cylinder, two ends of the U-shaped heat exchange tube group are communicated with the outside of the shell and are respectively communicated with the steam inlet tube and the 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 communicated with the heat exchange cylinder downwards, the top of the radial shell is provided with a conversion gas outlet, and the axial shell is provided with a raw material gas inlet;
an outer air cylinder is sleeved outside the central air distribution pipe, a heat transfer array pipe extending along the vertical direction is arranged between the central air distribution pipe and the outer air cylinder, the lower end of the heat transfer array pipe is connected with a refrigerant inlet pipe, and the refrigerant inlet pipe downwards penetrates through the partition plate end socket 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 is communicated with the conversion air outlet;
the upper end of the heat transfer array pipe is connected with a refrigerant outlet pipe, and the refrigerant outlet pipe upwards extends from the fixed part of the shell and forms 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 can be 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 converted 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 to generate secondary conversion gas, and the secondary conversion gas is discharged from the conversion gas outlet.
In this application, in order to guarantee the intensity of casing, radial casing adopts 14CrMoR material preparation, and the axial casing including the low head adopts 14CrMoR + S32168 composite board preparation, and wherein the S32168 material layer is located the inboard. 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 equipment is ensured.
In this application, the shell includes straight section of thick bamboo, upper cover and low head, and wherein upper cover links together with straight section of thick bamboo detachably to it is sealed to fill up to be equipped with omega between upper cover and the straight section of thick bamboo. The upper end socket is detachably mounted at the top of the straight cylinder, and the interior of the equipment can be mounted and overhauled through the upper end of the straight cylinder. Omega sealing is adopted to ensure the sealing performance of the equipment under high temperature and high pressure.
This application, the feed gas carries out preliminary reaction in the axial reaction section, can be favorable to COS to change into H with the temperature setting in the axial reaction section2And in the temperature range of S, other organic matters in the feed 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 operate for a long time. Because the axial reaction section has the advantage of replacing the catalyst, the reaction temperature of the axial reaction section is favorably set in a higher rangeThe produced product of gaseous organic matter reaction remains in the axial reaction section, impurity such as noxious material in the feed gas and dust also is remained in the axial reaction section in addition, make in this application, in the production process, after carrying out change many times to the catalyst in the axial reaction section, need change the catalyst in the centrifugal radial reaction section again, because the catalyst in the axial reaction section is changed and will be more convenient and swift than the side in the centrifugal radial reaction, and utilize this application, can shorten the change time of catalyst by a wide margin, improve the operating time of equipment.
The high reaction temperature of the axial reaction section is utilized to overheat the steam so as to improve the grade of the steam, and the produced superheated steam can be directly used as power steam.
This application can realize adiabatic reaction, accuse temperature reaction, produce saturated steam and carry out functions such as overheated to steam as a combined type tower ware. Under the condition of being beneficial to realizing the requirements of the technological process, the method is beneficial to the concise arrangement of the field equipment, the pipeline saving and the investment saving.
Further, a heat exchanger mounting opening used for the U-shaped heat exchange tube group to enter and exit is formed in the bottom of the shell, the lower end of the heat exchange tube is open and forms an inlet and an outlet of the heat exchanger, the heat exchanger mounting opening is opposite to the inlet and the outlet of the heat exchanger, and the U-shaped heat exchange tube group can freely enter and exit the heat exchange tube through the heat exchanger mounting opening and the inlet and the outlet of the heat exchanger. When the U-shaped heat exchange tube group needs to be replaced, the U-shaped heat exchange tube group can be drawn out 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 set is replaced with higher convenience, and the replacement of the U-shaped heat exchange tube set can be completed without entering the shell.
Further, in order to sufficiently absorb the reaction heat in the axial reaction section, a distance is formed between the lower end of the heat exchange cylinder and the inner surface of the bottom of the shell, and the distance forms a gas flow channel. Because the air flow channel is arranged at the lower end of the heat exchange cylinder, primary converted air can contact and exchange heat with the U-shaped heat exchange tube group to the maximum extent in the process of flowing through the heat exchange cylinder, and the heat exchange efficiency can be effectively improved.
Furthermore, the central gas distribution pipe extends upwards out of the top of the shell to form a raw gas inlet close to the route. The near-path inlet of the raw material can be used as a cold shock gas inlet of the centrifugal radial reaction section. In traditional equipment, generally set up the cold shock trachea alone, the cold shock gas gets into equipment back, directly gets into the reaction bed, reduces reaction temperature, but because the cold shock gas can't in time spread to the central zone of bed, causes the reaction bed in situ, the reaction temperature of local region can't effectively reduce. In this application, regard as the cold shock trachea with central gas distribution pipe simultaneously, the cold shock gas mixes at first with a change of gas that comes from the axial reaction section after getting into the reactor, directly reduces the temperature that changes gas once to make anti-straying more steady, can eliminate the overheated problem of local reaction effectively. After the design is adopted, the difference of the reaction temperature in the centrifugal radial reaction section can be reduced to 10-20 ℃ from the current 50-80 ℃.
Furthermore, in order to effectively control the reaction temperature of the axial reaction section, two axial bed layers are arranged in the axial reaction section, the two axial bed layers are arranged at intervals in the vertical direction, and the feed gas inlet is arranged on the upper side of the upper axial bed layer; and a cold shock gas inlet pipe is arranged between the two axial beds. A catalyst discharge pipe is provided corresponding to each axial bed layer 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 distributed around the heat exchange cylinder;
a cold shock gas distribution pipe is arranged between the two axial bed layers, 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 the two adjacent annular pipes, and the cold shock gas inlet pipe is connected to the cold shock gas distribution pipe; the cold shock gas distribution pipe is provided with cold shock gas holes. The annular pipe and the connecting pipe are both provided with cold shock air holes.
The second cold shock gas enters the cold shock gas distribution pipe through the cold shock gas holes and then enters the two axial bed layers, and in order to enable the cold shock gas to uniformly enter the two axial bed layers, 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.
Because the refrigerant inlet pipe has occupied the best position of cold shock gas distribution pipe, for the evenly distributed of guaranteeing the second cold shock gas, in this application, the annular pipe has been established to the cover on the refrigerant inlet pipe, makes cold shock gas distribution pipe furthest arrange on the best position, makes the cold shock gas of second evenly distributed.
Further, 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 the steam inlet. This design can make the reactor in this application carry out continuous heating to same water source, at first heats the soft water in the steam pocket by centrifugal radial reaction section and generates saturated water, then is overheated to the saturated steam that the steam pocket flash evaporation was gone out by axial reaction section again, produces superheated steam to make full use of reaction heat reaches the target of producing superheated steam concurrently.
Because the same steam drum is used when producing saturated water and superheated steam, 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 items, 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 converted gas; the primary conversion gas can enter the heat exchange cylinder through the gas flow channel, and then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion to generate secondary conversion gas, 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 pocket enters the heat transfer tubes through the refrigerant inlet, superheated water is formed after the heat transfer of the centrifugal radial reaction section is absorbed, and the superheated water is discharged from the refrigerant outlet and returns to the steam pocket; superheated water in the steam pocket 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 of transformation of the axial reaction section and then becomes superheated steam.
In the conversion process, the raw material gas is subjected to primary reaction in the axial reaction section, and the temperature in the axial reaction section can be set to be favorable for converting COS into H2And in the temperature range of S, other organic matters in the feed 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 operate for a long time. Because the axial reaction section has the advantage of changing the catalyst, consequently when setting up the reaction temperature of axial reaction section in higher within range, be favorable to remaining the produced product of gaseous organic matter reaction in the axial reaction section, impurity such as noxious material and dust in the feed gas also is reserved in the axial reaction section in addition, make in this application, in process of production, after axial reaction section internal catalyst carries out the change many times, need change centrifugal radial reaction section internal catalyst again, because the axial reaction section internal catalyst is changed and will be more convenient and swift than the side in centrifugal radial reaction, and utilize this application, can shorten the change time of catalyst by a wide margin, improve equipment's operating time.
The high reaction temperature of the axial reaction section is utilized to overheat the steam so as to improve the grade of the steam, and the produced superheated steam can be directly used as power steam.
Furthermore, the first cold shock gas enters the central gas distribution pipe from a raw gas near-path inlet at the top of the shell to adjust the temperature in the centrifugal radial reaction section. And 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 this application, regard as the cold shock trachea with central gas distribution pipe simultaneously, the cold shock gas mixes at first with a change of gas that comes from the axial reaction section after getting into the reactor, directly reduces the temperature that changes gas once to make anti-straying more steady, can eliminate the overheated problem of local reaction effectively. After the design is adopted, the difference of the reaction temperature in the centrifugal radial reaction section can be reduced to 10-20 ℃ from the current 50-80 ℃.
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 conversion 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 structural diagram of an embodiment of the present invention.
Detailed Description
Referring to fig. 1, the reactor for CO shift and superheated steam with adiabatic series isothermal reaction comprises a housing 10 extending along a vertical direction, wherein the housing 10 specifically comprises a straight cylinder 11, an upper end enclosure 12 positioned at the top of the straight cylinder, and a lower end enclosure 13 positioned at the bottom of the straight cylinder. The upper end enclosure 12 and the straight cylinder 11 are detachably connected together through bolts, omega seals are arranged between the upper end enclosure and the straight cylinder in a cushioning mode, and the lower end enclosure is directly welded on the straight cylinder.
A partition plate head 14 is provided in the housing, and this partition plate head 14 is welded to the inner wall of the straight tube 11 and divides the housing 10 into a radial shell on the upper side and an axial shell on the lower side.
A centrifugal radial reaction section 101 is provided within the radial housing and an axial reaction section 102 is provided within the axial housing.
A heat exchange cylinder 71 is axially arranged at the center of the axial shell, and a U-shaped heat exchange tube group 61 is installed in the heat exchange cylinder 71. The bottom of the lower end enclosure 13 is provided with a bottom hole, a flange 17 is welded on the bottom hole, a heat exchange tube plate 63 is hermetically installed on the lower side of the flange 17 by using bolts, and a heat exchange end enclosure 62 is welded on the lower side of the heat exchange tube plate 63. A dividing plate 64 is welded in the heat exchange seal head 62 and positioned in the heat exchange seal head 62 and welded between the heat exchange seal head and the heat exchange tube plate, an inner cavity between the heat exchange seal head 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 seal head and communicated with the inlet cavity, and a steam outlet pipe 66 is welded on the heat exchange seal head and communicated with the outlet cavity.
The two 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 for the U-shaped heat exchange tube group to enter and exit.
The lower end of the heat exchange cylinder is open and forms a heat exchanger inlet and a heat exchanger outlet, and the heat exchanger inlet and the heat exchanger outlet are opposite to a heat exchanger mounting opening. The lower end of the cartridge is spaced from the inner surface of the bottom of the shell by a distance 72, the distance 72 forming an air flow path.
When the U-shaped heat exchange tube group 61 needs to be replaced, the bolts connecting the flange 17 and the heat exchange tube plate 63 are disassembled, then the U-shaped heat exchange tube group 61, the heat exchange tube plate 63 and the heat exchange end enclosure 62 are integrally disassembled, and are drawn out from the shell through the central hole of the flange 17 and the inlet and outlet of the heat exchanger, and then the new U-shaped heat exchange tube group 61, the new heat exchange tube plate 63 and the new heat exchange end enclosure 62 are replaced. Namely, the U-shaped heat exchange tube group can freely enter and exit the heat exchange cylinder through the heat exchanger mounting opening 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 is coaxially arranged with the heat exchange cylinder 71 and connected together, and the central gas distribution pipe 31 is communicated with the heat exchange cylinder 71 downwards.
An 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 tubes 21 extending along the vertical direction, an upper tube plate 44 and a lower tube plate 43 are arranged corresponding to each heat transfer pipe group 20, and two ends of each heat transfer tube 21 are respectively welded on the upper tube plate 44 and the lower tube plate 43. An upper inner seal head 45 is installed on the upper side of the upper tube plate 44, a refrigerant outlet pipe 46 is installed on the upper inner seal head, and the refrigerant outlet pipe 46 extends upwards out of the upper seal head to form a refrigerant outlet 461. 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 both shown in the attached drawing, and the prior art can be adopted.
A lower inner head 42 is installed at the lower side of the lower tube plate 43, a refrigerant inlet pipe 41 is installed on the lower inner head, and the refrigerant inlet pipe 41 penetrates through the partition plate head and the axial reaction section downwards, extends out of the lower head and forms a refrigerant inlet 411. The refrigerant inlet pipes 41 are uniformly arranged around the heat exchange cylinder 71.
Two axial beds are arranged in the axial reaction section, the two axial beds are respectively a first axial bed 51 and a second axial bed 56, and the first axial bed 51 is positioned 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 provided on the upper side of the first axial bed 51, i.e., the feed gas inlet is provided 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 along 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 bed layers, 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 the two adjacent annular pipes, and the cold shock gas inlet pipe 58 is connected to the cold shock gas distribution pipe; the cold quenching air holes are formed in the cold quenching air distribution pipe, and particularly in the embodiment, the cold quenching air holes are formed in the annular pipe and the connecting pipe.
The upper end closure is provided with a shift gas outlet 16, and an annular space is formed between the outer cylinder and the shell and is communicated with the shift gas outlet.
The central gas distribution pipe 31 extends upwards out of the upper end enclosure to form a raw gas inlet 313 close to the route.
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 converted 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 to generate secondary conversion gas, 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 participates in the reaction in the centrifugal radial reaction section, and adjusts the reaction temperature in the centrifugal radial reaction section. 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 a hot water outlet pipe 81 of a drum 80, the refrigerant outlet 461 is connected to a hot water inlet pipe 82 of the drum, a steam discharge pipe 83 of the drum is communicated with a steam inlet 83, and a soft water supplement pipe 84 is installed on the drum 80.
The following describes a gas shift process using the above reactor, which includes 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 converted gas; the primary conversion gas can enter the heat exchange cylinder through the gas flow channel, and then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion to generate secondary conversion gas, 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 pocket enters the heat transfer tubes through the refrigerant inlet, superheated water is formed after the heat transfer of the centrifugal radial reaction section is absorbed, and the superheated water is discharged from the refrigerant outlet and returns to the steam pocket; superheated water in the steam pocket 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 of transformation of the axial reaction section and then becomes superheated steam.
The first cold shock gas enters the central gas distribution pipe from the raw gas near-path inlet at the top of the shell to adjust the reaction temperature in the centrifugal radial reaction section. And 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 of the axial reaction section was 395-405 ℃ and the reaction temperature of the centrifugal radial reaction section was 285-290 ℃. Saturated steam flashed from the steam drum 80 passes through the U-shaped heat exchange tube group to become superheated steam with the temperature of 400 ℃, and the inlet temperature of the saturated steam is 250 ℃.
Claims (10)
1. A reactor for CO conversion with adiabatic series isothermal and producing superheated steam is characterized in that,
the device comprises a shell extending along the vertical direction, wherein a partition plate end enclosure is arranged in the shell and divides the shell into a radial shell positioned on the upper side and an axial shell positioned on 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 arranged at the central part of the axial shell along the axial direction, and the heat exchange cylinder is provided with an airflow channel; a U-shaped heat exchange tube group is arranged in the heat exchange cylinder, two ends of the U-shaped heat exchange tube group are communicated with the outside of the shell and are respectively communicated with the steam inlet tube and the 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 communicated with the heat exchange cylinder downwards, the top of the radial shell is provided with a conversion gas outlet, and the axial shell is provided with a raw material gas inlet;
an outer air cylinder is sleeved outside the central air distribution pipe, a heat transfer array pipe extending along the vertical direction is arranged between the central air distribution pipe and the outer air cylinder, the lower end of the heat transfer array pipe is connected with a refrigerant inlet pipe, and the refrigerant inlet pipe downwards penetrates through the partition plate end socket 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 is communicated with the conversion air outlet;
the upper end of the heat transfer array pipe is connected with a refrigerant outlet pipe, and the refrigerant outlet pipe upwards extends from the fixed part of the shell and forms 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 converted 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 to generate secondary conversion gas, and the secondary conversion gas is discharged from the conversion gas outlet.
2. The reactor according to claim 1,
the bottom of the shell is provided with a heat exchanger mounting opening used for the U-shaped heat exchange tube group to enter and exit, the lower end of the heat exchange tube is open and forms a heat exchanger inlet and a heat exchanger outlet, the heat exchanger mounting opening is over against the heat exchanger inlet and the heat exchanger outlet, and the U-shaped heat exchange tube group can freely enter and exit the heat exchange tube through the heat exchanger mounting opening and the heat exchanger inlet and the heat exchanger outlet.
3. The reactor according to claim 3,
the lower end of the heat exchange cylinder is spaced from the inner surface of the bottom of the shell to form an air flow passage.
4. The reactor according to claim 1,
the central gas distribution pipe extends upwards out of the top of the shell to form a raw gas inlet close to the route.
5. The reactor according to claim 1,
two axial bed layers are arranged in the axial reaction section, the two axial bed layers are arranged at intervals in the vertical direction, and the feed gas inlet is arranged on the upper side of the upper axial bed layer; and a cold shock gas inlet pipe is arranged between the two axial beds.
6. The reactor according to claim 5,
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 cylinder;
a cold shock gas distribution pipe is arranged between the two axial bed layers, 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 the two adjacent annular pipes, and the cold shock gas inlet pipe is connected to the cold shock gas distribution pipe; the cold shock gas distribution pipe is provided with cold shock gas holes.
7. The 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 the steam inlet.
8. A gas shift process using the reactor of any one of claims 1 to 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 converted gas; the primary conversion gas can enter the heat exchange cylinder through the gas flow channel, and then the central gas distribution pipe enters the centrifugal radial reaction section for secondary conversion to generate secondary conversion gas, 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 pocket enters the heat transfer tubes through the refrigerant inlet, superheated water is formed after the heat transfer of the centrifugal radial reaction section is absorbed, and the superheated water is discharged from the refrigerant outlet and returns to the steam pocket; superheated water in the steam pocket 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 of transformation of the axial reaction section and then becomes superheated steam.
9. The gas shift process according to claim 8,
the first cold shock gas enters the central gas distribution pipe from the raw gas near-path inlet at the top of the shell to adjust the temperature in the centrifugal radial reaction section.
10. The gas shift process according to claim 8 or 9,
the reaction temperature of the axial reaction section is 390-410 ℃, and the reaction temperature of the centrifugal radial reaction section is 280-295 ℃.
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