CN111732075B - Composite heat-insulating serial temperature-control shift converter device and shift process - Google Patents
Composite heat-insulating serial temperature-control shift converter device and shift process Download PDFInfo
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- CN111732075B CN111732075B CN202010596509.2A CN202010596509A CN111732075B CN 111732075 B CN111732075 B CN 111732075B CN 202010596509 A CN202010596509 A CN 202010596509A CN 111732075 B CN111732075 B CN 111732075B
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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
- C01B3/06—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
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
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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
- C01B3/06—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
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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
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The invention discloses a composite heat-insulating serial temperature-controlling converter device, which comprises a heat-insulating reaction part, a temperature-controlling reaction part and a connecting part connected between the heat-insulating reaction part and the temperature-controlling reaction part; the adiabatic reaction part comprises a first shell, an inner cylinder arranged in the first shell, a first annular gap is formed between the first inner cylinder and the first shell, and a cold shock gas pipe, a raw gas inlet pipe and a section of conversion gas outlet pipe are arranged on the first shell; the temperature control reaction part comprises a second shell, an air distribution cylinder is arranged in the second shell, a second annular space is formed between the air distribution cylinder and the second shell, and a steam-water mixture outlet pipe, a two-section conversion air inlet pipe, a water inlet pipe and a conversion air outlet pipe are arranged on the second shell. The heat insulation reaction part and the temperature control reaction part are independent relatively, so that the occupied area can be reduced. The application also discloses a change process using the composite heat-insulating serial control temperature conversion furnace device. The process can reduce COS in the shift gas and minimize methanation side reaction.
Description
Technical Field
The invention relates to a composite heat-insulating serial control temperature conversion furnace device, which adopts a conversion process of the conversion furnace device.
Background
In coal chemical industry, the raw material gas obtained after gasification of pulverized coal is subjected to a shift reaction to generate shift gas, so that CO in the raw material gas is converted into CO 2 Simultaneous generation of H 2 At present, in the conversion reaction process, steam is generally CO-produced, and in order to meet the needs of various pressure steam of the self, the conversion reaction is used for obtaining various pressure steam for production, so that the reaction time is often too long, the CO conversion cannot be effectively improved, and the production process flow is long.
At present, because the flow of the CO conversion reaction is longer, a plurality of reactors are generally arranged according to different reaction temperatures, and the reactors are connected by adopting pipelines, the equipment arrangement mode has the advantages of flexible and convenient cooling and heat exchange modes among the equipment, and the equipment is convenient to overhaul, but the arrangement area of the whole set of device is larger, and the pipelines are more.
In order to reduce the floor space, a single-furnace multistage reactor is developed, namely, a heat insulation section and a control section are arranged in one furnace, or a plurality of heat insulation sections are arranged, and the reactor has the advantages of small floor space, few pipelines, complex structure, high manufacturing cost and inconvenient filling and discharging of the catalyst.
In addition, in the coal gasification technology adopted at present, the dry basis volume ratio of CO in the produced synthetic gas is generally more than 60%, and the water-gas ratio is generally 0.7-1.0. When the synthesis gas is used for producing the synthesis ammonia feed gas, CO in the synthesis gas needs to be converted into hydrogen to the maximum extent, and a high water-gas ratio of more than 1.2 is generally required to meet the requirement, but the high water-gas ratio can enlarge the volume of the synthesis gas, a larger shift reactor is required, the reaction is more severe, the reaction is extremely easy to generate a temperature runaway phenomenon, and the control of the production process becomes more complex. The large-scale shift reactor is high in manufacturing cost and maintenance cost. The use of more costly shift reactors and the production of shift gas under complex control conditions correspondingly increases the cost. Meanwhile, the water-air ratio is high, so that the consumption of steam is increased, and the cost is increased.
It is also a real problem how to make reasonable use of existing synthesis gas and to produce shift gas at lower costs.
Disclosure of Invention
In order to solve the above problems, the present invention firstly proposes a composite heat-insulating serial control temperature conversion furnace device, which comprises a heat-insulating reaction part, a temperature-controlling reaction part and a connecting part connected between the heat-insulating reaction part and the temperature-controlling reaction part, wherein the heat-insulating reaction part is positioned above the temperature-controlling reaction part;
the heat insulation reaction part comprises a first shell extending along the vertical direction, wherein the first shell is cylindrical, a first inner part is arranged in the first shell, and comprises an inner cylinder extending along the vertical direction, a first inner lower seal head hermetically arranged at the lower end of the inner cylinder and a top grid arranged at the upper end of the inner cylinder; an annular first annular gap is formed between the first inner cylinder and the first shell, a gas distribution cavity is formed between the top grille and the top of the first shell, and a gas inlet cavity is formed between the first inner lower seal head and the bottom of the first shell; the upper end and the lower end of the first annular gap are respectively communicated with the air distribution cavity and the air inlet cavity; the first inner piece is supported at the bottom of the first shell, and the first inner piece is in sliding connection with the inner peripheral wall of the first shell, so that the first inner piece can freely stretch and retract in the vertical direction;
the first shell is provided with a cold shock air pipe, and the outlet end of the cold shock air pipe is positioned in the inner cavity of the inner cylinder;
a raw gas inlet pipe and a section of conversion gas outlet pipe are arranged at the bottom of the first shell, wherein the raw gas inlet pipe is communicated with the gas inlet cavity, one end of the section of conversion gas outlet pipe is communicated with the inner cavity of the inner cylinder, and the other end of the section of conversion gas outlet pipe extends downwards out of the first shell;
the temperature control reaction part comprises a second shell extending along the vertical direction, the second shell is cylindrical, a second internal part is arranged in the second shell, the second internal part comprises an air distribution cylinder extending along the vertical direction, an upper tube plate arranged at the upper end of the air distribution cylinder, a lower tube plate arranged at the lower end of the air distribution cylinder, and a heat exchange tube array is arranged between the upper tube plate and the lower tube plate; a second annular gap is formed between the air distribution cylinder and the second housing, and an air distribution hole which is communicated with the second annular gap and the inner cavity of the air distribution cylinder is formed in the air distribution cylinder;
a steam-water mixture outlet pipe and a two-section conversion gas inlet pipe are arranged at the top of the second shell, a water inlet pipe is arranged at the bottom of the second shell, the upper end of the heat exchange tube array is communicated with the steam-water mixture outlet pipe, and the lower end of the heat exchange tube array is communicated with the water inlet pipe; the second-stage conversion gas inlet pipe is communicated with the second annular gap;
a conversion gas discharge pipe is arranged at the bottom of the second shell, a conversion gas concentration pipe is arranged at the central part of the gas cylinder and extends along the vertical direction, the top end of the conversion gas concentration pipe is accommodated in the inner cavity of the gas cylinder, and the lower end of the conversion gas concentration pipe extends downwards and is communicated with the conversion gas discharge pipe; the tube wall of the conversion gas concentration tube is provided with a through hole-shaped air hole communicated with the inner cavity of the gas distribution tube.
The converter device is provided with two relatively independent heat insulation reaction parts and a temperature control reaction part, so that the occupied area is reduced, when the converter device is used for producing the conversion gas, raw gas firstly enters the heat insulation reaction part at the top for reaction and then enters the temperature control reaction part downwards for reaction, the heat insulation reaction part is arranged above the temperature control reaction part, when corresponding pipelines are arranged, the converter device can be relied on, and when the independent heat insulation reactor and the independent temperature control reactor are arranged, corresponding installation platforms are required to be respectively arranged for installing the heat insulation reactor and the temperature control reactor, so that the problems of high construction cost, long construction period and the like are caused.
The heat-insulating reaction part in the shift converter device is an axial reaction section and is provided with a first annular gap, and during production, raw gas firstly enters the gas distribution cavity through the raw gas inlet pipe, then rises into the gas distribution cavity along the first annular gap and then enters the first inner cylinder downwards to react. Because the first internal part is supported at the bottom of the first shell and can freely stretch and retract along the vertical direction, when the heat insulation reaction part works, the first shell cannot be influenced by the internal stress of the internal part, which changes due to expansion and contraction, so that the first shell is only influenced by the internal pressure generated by self deformation.
The temperature control reaction part in the shift converter device is a radial reaction section, a second inner part is arranged in the second shell, a second annular space is arranged between the air distribution cylinder of the second inner part and the second shell, when the temperature control reaction part works, a section of shift air discharged from the heat insulation reaction part enters the second shell through a second section of shift air inlet pipe at the top of the second shell, then flows downwards along the second annular space, enters the inner cavity of the air distribution cylinder through the air distribution cylinder for reaction, and the reacted air is discharged downwards through a shift air concentration pipe and enters the next process.
Because of the blocking effect of the first section of conversion gas in the second annular gap, the temperature of the second shell is lower than that of the inner cavity of the second inner cylinder, the temperature of the second shell is reduced, and the deformation of the second shell is reduced, so that the service life of the equipment is ensured.
Specifically, two layers of catalyst support plates, namely a first catalyst support plate and a second catalyst support plate, are arranged in the inner cylinder along the height direction, the first catalyst support plate is positioned above the second catalyst support plate, and an intermediate grille is arranged between the first catalyst support plate and the second catalyst support plate; a first catalyst cavity is formed in front of the first catalyst support plate and the top grid, a second catalyst cavity is formed between the middle grid and the second catalyst support plate, a cold shock cavity is formed between the first catalyst support plate and the middle grid, and the outlet end of the cold shock air pipe is positioned in the cold shock cavity; the first catalyst cavity and the second catalyst cavity are filled with catalyst, and no catalyst is filled in the cold shock cavity;
corresponding to each layer of catalyst supporting plate, a catalyst discharging pipe is arranged, and each catalyst discharging pipe extends downwards and extends out of the first shell from the bottom of the first shell.
The adiabatic reaction part is sequentially provided with a first catalyst cavity, a cold shock cavity and a second catalyst cavity, wherein the cold shock cavity is used as a cold shock gas distribution cavity. The raw material gas is divided into two paths and enters the adiabatic reaction part, wherein the first path of raw material gas sequentially passes through the first catalyst cavity, the cold shock cavity and the second catalyst cavity from top to bottom, and a large amount of CO is converted into CO after the first path of raw material gas passes through the first catalyst cavity 2 The second path of raw material gas is used as cold shock gas to enter the cold shock cavity, reacts along with the first raw material gas entering the second catalyst cavity, and is arranged between the first catalyst cavity and the second catalyst cavity, the second path of raw material gas entering the cold shock cavity can also reduce the temperature of the first catalyst cavity, so that the overhigh reaction temperature is avoided, after the raw material gas passes through the reaction of the first catalyst cavity, the CO content in the first path of raw material gas is greatly reduced, and after the second path of raw material gas enters the cold shock cavity, the raw material gas also mainly enters the second catalyst cavity to react, so that the raw material gas reacts more uniformly in the adiabatic reaction part.
Further, the cold shock air pipe and the inner cylinder are coaxially arranged, the inlet end of the cold shock air pipe extends out of the top of the first shell upwards, and the outlet end of the cold shock air pipe freely penetrates through the top grid and the first catalyst supporting plate downwards and then enters the cold shock cavity.
The design can reduce the limit of the free expansion and contraction of the cold shock tube to the first shell, and reduce the internal stress generated when the first shell expands with heat and contracts with cold. When the heat-insulating reaction part works, the first outer shell and the first internal part are expanded to different degrees at high temperature, so that after the cold shock air pipe freely passes through the top grid and the first catalyst supporting plate, the cold shock air pipe and the first internal part can be ensured to be free of contact, when the cold shock air pipe is deformed, the first internal part such as the top grid and the first catalyst supporting plate cannot be influenced, and meanwhile, the deformation of the first internal part cannot influence the deformation of the cold shock air pipe, so that each part can freely stretch and retract to the maximum extent, the aggregation of internal stress is reduced, and the safe use of equipment is ensured.
Specifically, a discharge pipe is sleeved on the conversion gas concentration pipe, the upper end of the discharge pipe is connected to the lower pipe plate, and the lower end of the discharge pipe is hermetically arranged at the bottom of the second shell; a discharging cavity is arranged at the bottom of the second shell, a discharging hole communicated with the discharging cavity is formed in the discharging pipe, a discharging pipe communicated with the discharging cavity is arranged at the outer side of the second shell, a circular discharging cavity is formed between the discharging pipe and the conversion gas collecting pipe, and the discharging cavity is communicated with the inner cavity of the gas distribution cylinder.
The design can smoothly discharge the catalyst in the temperature control reaction part, when the catalyst in the temperature control reaction part is required to be discharged, the catalyst in the air distribution cylinder can enter the discharge cavity through the discharge cavity and then is discharged through the discharge pipe.
Further, a mounting hole for inserting the shift gas collecting tube into the gas cylinder is provided at the center of the upper tube plate, and a sealing cover is detachably mounted on the mounting hole, the sealing cover comprises a flange and a sealing cover connected to the flange, the sealing cover is in a shape of a circular arc protruding downward.
By utilizing the mounting hole, the conversion gas concentration tube can be smoothly inserted into the gas cylinder for mounting, and the arc-shaped sealing cover on the sealing cover can be smoothly mounted on the mounting hole, so that the arc-shaped sealing cover can bear larger pressure, and the thickness of the sealing cover is reduced.
Secondly, the application also provides a conversion process, which is carried out by the composite heat-insulating serial control temperature conversion furnace device, and comprises the following steps:
primary adiabatic conversion: the raw gas is detoxified after passing through the heat exchanger, the detoxified raw gas is divided into two paths, one path is feed gas, the other path is cold shock gas, the feed gas enters the air inlet cavity of the adiabatic reaction part through the raw gas inlet pipe, then flows upwards along the first annular gap to enter the air distribution cavity, and then enters the inner cavity of the inner cylinder through the top grid to react; cold shock gas enters the inner cavity of the inner cylinder through a cold shock gas pipe, and is mixed with feed gas to react; the raw material gas is reacted to generate a first-stage conversion gas, and the first-stage conversion gas is discharged from a first-stage conversion gas outlet pipe;
and (3) secondary temperature control conversion: the first-stage conversion gas enters the mixer, the adjusting steam and adjusting water enter the mixer to adjust the water-gas ratio and the temperature of the first-stage conversion gas, the first-stage conversion gas discharged from the mixer enters the temperature control reaction part through the second-stage conversion gas inlet pipe, then enters the inner cavity of the gas distribution cylinder through the second annular gap to react to generate the second-stage conversion gas, and the second-stage conversion gas enters the conversion gas concentration pipe and then is discharged through the conversion gas discharge pipe; the two-stage converter enters a heat exchanger to heat the raw material gas;
saturated water in the steam drum enters the heat exchange tube by the water inlet pipe, exchanges heat and then is discharged by the steam-water mixture outlet pipe to enter the steam drum to produce byproduct steam.
In the shift process, raw gas firstly generates a shift gas after reaction of an adiabatic reaction part, then the water-gas ratio and the temperature of the shift gas are regulated, and the adiabatic reaction part can adopt high-temperature reaction to improve the operating temperature of a temperature control reaction part and improve the water spraying amount so as to reduce COS in the shift gas, and simultaneously can adopt low water-gas ratio to minimize methanation side reaction.
Further, the by-product steam of the drum is used as the conditioning steam.
The byproduct steam of the steam drum is returned to the conversion system as conditioning steam, so that the consumption of external energy sources can be reduced.
Specifically, in the raw material gas, the volume ratio of dry CO is 62-75% and the water-gas ratio is 0.48-0.54;
the inlet temperature of the feed gas and the cold shock gas entering the adiabatic reaction part is 250-260 ℃;
in the adiabatic reaction part, the reaction pressure is 6.0-6.2MPaG; MPaG represents gauge pressure;
the outlet temperature of the first-stage conversion gas in the adiabatic reaction part is 430-435 ℃;
the volume ratio of the dry basis CO of the one-stage converted gas is 31-37%,
after the water is supplemented to the first-stage converted gas, the water-gas ratio is 0.58-0.66;
the inlet temperature from the first-stage conversion gas to the temperature-control reaction part is 290-298 ℃;
the outlet temperature of the second-stage conversion gas in the temperature-control reaction part is 315-330 ℃;
the volume ratio of dry-base CO in the two-stage conversion gas is 2.5-3.5%;
the pressure of the byproduct steam in the steam drum is 6.3-6.9MPaG.
Under the limitation of the above process conditions, when the raw material gas reacts in the adiabatic reaction part, the low water-gas ratio is adopted, the reaction temperature of the adiabatic reaction part reaches 430 ℃, the reaction temperature and the water spraying amount of the temperature-control reaction part can be increased, COS in the gas can be reduced, and the methanation side reaction can be minimized when the adiabatic reaction part reacts in the low water-gas ratio, wherein the COS volume ratio in the two-stage conversion gas is 0.0014% dry basis, and the methane volume ratio is 0.038% dry basis.
The pressure of the byproduct steam in the steam drum can be adapted to the temperature in the temperature-controlled reaction part, so that the self-produced steam can be naturally added into the reaction system, and the temperature in the temperature-controlled reaction part can be conveniently controlled.
Due to the adoption of the operation with low water-gas ratio, a large amount of steam can be saved, the condensation water quantity is reduced, and the methanation side reaction is well inhibited.
Further, the steam drum produces only one kind of steam in order to make the pressure of the byproduct steam of the steam drum maximally compatible with the temperature in the temperature-controlled reaction part.
Drawings
FIG. 1 is a schematic diagram of an embodiment of a composite adiabatic series control temperature shift furnace apparatus.
Fig. 2 is an enlarged view of a portion B in fig. 1, specifically, a schematic structural view of an adiabatic reaction portion.
Fig. 3 is a left side view of fig. 2.
Fig. 4 is an enlarged view of a portion C in fig. 1, specifically, a schematic structural view of the temperature-controlled reaction portion.
Fig. 5 is a left side view of fig. 4.
Fig. 6 is an enlarged view of a portion a in fig. 5.
Fig. 7 is a flow chart of a shift process.
Detailed Description
Referring to fig. 1 to 6, a composite adiabatic serial temperature-controlled shift converter device includes an adiabatic reaction portion 100, a temperature-controlled reaction portion 300, and a connection portion 200 connected between the adiabatic reaction portion 100 and the temperature-controlled reaction portion 300, wherein the adiabatic reaction portion 100 is located above the temperature-controlled reaction portion 300.
The adiabatic reaction portion 100 includes a first housing 10 extending in a vertical direction, the first housing 10 having a cylindrical shape, and specifically includes a first cylindrical body 11 having a cylindrical shape, and a first upper head 12 and a first lower head 13 mounted on upper and lower ends of the first cylindrical body 11.
Inside the first casing 10, there is provided a first inner member including an inner cylinder 21 extending in a vertical direction, a first inner lower head 22 sealingly mounted at a lower end of the inner cylinder 21, and a top grill 23 mounted at an upper end of the inner cylinder 21, the first inner lower head 22 being supported on the first lower head 13 via legs 221. An annular first annular gap is formed between the first inner cylinder 21 and the first cylinder 11 of the first housing 10, a gas distribution chamber 101 is formed between the top grille 23 and the top of the first housing, and a gas inlet chamber 102 is formed between the first inner lower head 22 and the bottom of the first housing. The upper end and the lower end of the first annular space are respectively communicated with the air distribution cavity 101 and the air inlet cavity 102. The upper portion outside the inner tube 21 is installed a supporting block 211, and this supporting block 211 supports and presses on the inner wall of first barrel 11, makes and forms first annular space between first barrel 11 and the inner tube 21, and when thermal expansion, the inner tube can extend upwards along vertical direction, and when meeting cold shrink, the inner tube can retract downwards along vertical direction, and when inner tube extends or retracts along vertical direction, the supporting block slides from top to bottom along the inner wall of first barrel 11. The first inner piece is supported at the bottom of the first shell, and the first inner piece is connected with the inner peripheral wall of the first shell in a sliding way, so that the first inner piece can freely stretch and retract in the vertical direction.
Along the height direction, two layers of catalyst support plates are arranged in the inner cylinder, namely a first catalyst support plate 24 and a second catalyst support plate 26, the first catalyst support plate 24 is positioned above the second catalyst support plate 26, and an intermediate grille 25 is arranged between the first catalyst support plate and the second catalyst support plate. The first catalyst supporting plate 24 and the top grille 23 are formed with a first catalyst chamber 241, a second catalyst chamber 261 is formed between the middle grille 25 and the second catalyst supporting plate 26, and a cooling chamber 251 is formed between the first catalyst supporting plate and the middle grille 25; the first catalyst cavity and the second catalyst cavity are filled with catalyst, and no catalyst is filled in the cold shock cavity.
Corresponding to each layer of catalyst supporting plate, a catalyst discharging pipe is arranged, and each catalyst discharging pipe extends downwards and extends out of the first shell from the bottom of the first shell. In this embodiment, the two catalyst discharging pipes are a first catalyst discharging pipe 331 and a second catalyst discharging pipe 332, wherein the first catalyst discharging pipe 331 penetrates the first catalyst supporting plate 24 upward and then communicates with the first catalyst chamber 241, so as to discharge the catalyst in the first catalyst chamber 241. The second catalyst discharging pipe 332 penetrates through the second catalyst supporting plate 26 upwards and then is communicated with the second catalyst cavity 261, and is used for discharging catalyst in the first catalyst cavity 261.
The cold shock air pipe 35 is installed on the first upper end enclosure 12, extends along the vertical direction and is coaxially arranged with the inner cylinder 21, the inlet end 351 of the cold shock air pipe 35 extends upwards out of the first upper end enclosure 12, and the outlet end of the cold shock air pipe extends downwards into the cold shock cavity 251 and is provided with an air distribution head 352. I.e. the other end of the cold shock tube extends downwards into the central part of the inner cavity of the inner cylinder. The outer sleeve 358 is sleeved on the cold shock tube 35 and is vertically arranged on the top grid 23 and the first catalyst supporting plate 24, and a gap is reserved between the cold shock tube and the outer sleeve 358, so that the outlet end of the cold shock tube freely passes through the top grid and the first catalyst supporting plate downwards and then enters the cold shock cavity. The cold shock pipe can freely stretch out and draw back along the vertical direction when expanding with heat and contracting with cold.
The gas distribution head 352 is located at the center of the inner cavity of the inner cylinder, specifically in this embodiment, the gas distribution head 352 specifically includes a conical tube 353 installed on the cold shock tube, the small end of the conical tube 353 faces upwards and is installed on the cold shock tube 35, a plurality of vertical rods 354 extending along the vertical direction are welded on the large end of the conical tube 353, the vertical rods 354 are arranged at intervals along the end face of the large end of the conical tube, a plurality of distribution rods 355 are fixed on each vertical rod, and a plurality of distribution rods 355 are arranged at intervals along the vertical direction, so that the distribution rods and the vertical rods are formed into a grid shape together, an arc plate 356 protruding upwards is installed at the lower end of the vertical rod, and the arc plate 356 enables gas sprayed from the cold shock tube to flow downwards along the inclined direction.
The raw gas inlet pipe 32 is installed on the first lower head 13 and communicates with the gas inlet chamber 102. A section of conversion gas outlet pipe 31 is arranged on the first lower sealing head 13, one end of the section of conversion gas outlet pipe 31 is communicated with the inner cavity of the inner cylinder, and the other end of the section of conversion gas outlet pipe extends downwards out of the first lower sealing head 13. Specifically in this embodiment, one end of the first section of the shift gas outlet pipe 31 penetrates through the first lower end enclosure 13 and the first inner lower end enclosure 22 in turn, then extends into the inner cavity of the first inner lower end enclosure 22, and is communicated with the inner cavity of the inner cylinder through the second catalyst support plate 26. The other end of the raw gas inlet pipe 32 is located outside the first housing. A protective cover 313 is installed at one end of the first section of shift gas outlet pipe 31 located in the inner cavity of the first inner lower seal head 22, so as to prevent the falling catalyst from entering the first section of shift gas outlet pipe 31.
A first upper manhole 121 is mounted on the first upper head 12, and a first lower manhole 131 is mounted on the first lower head 13.
The temperature-controlled reaction part 300 includes a second housing 60 extending in a vertical direction, the second housing 60 being cylindrical, the second housing specifically including a cylindrical second cylinder 61 and second upper and lower seal heads 62 and 63 mounted on upper and lower ends of the second cylinder 61.
A second inner member including a gas cylinder 71 extending in a vertical direction, an upper tube plate 72 mounted on an upper end of the gas cylinder 71, and a lower tube plate 76 mounted on a lower end of the gas cylinder is provided in the second housing 60. A second inner upper head 73 is mounted on the upper side of the upper tube sheet 72 and a second inner lower head 77 is mounted on the lower side of the lower tube sheet 76.
The heat exchange tubes 75 are mounted between and extend through the upper and lower tube sheets, respectively. The lower end of the steam-water mixture outlet pipe 85 is communicated with the inner cavity of the second inner upper seal head 73, and the upper end extends upwards to form the second upper seal head 62 and then is provided with a steam-water discharge pipe 851. The water inlet pipe 86 is arranged on the second lower sealing head 63 and is communicated with the inner cavity of the second inner lower sealing head 77, so that the water inlet pipe 86 is communicated with the steam water discharge pipe 851 through a heat exchange tube. The inlet tube 86 extends obliquely downward and then extends horizontally to form a horizontal tube section 861.
A drain 863 is mounted on the underside of the horizontal tube section 861 and a water inlet 862 is mounted on the upper side.
A pipe cap 867 is installed at the end of the horizontal pipe section 861, a steam orifice plate 865 is installed between the pipe cap 867 and the horizontal pipe section, a plurality of steam holes are formed in the steam orifice plate 865, a perforated pipe 866 is installed at one side facing away from the pipe cap corresponding to each steam hole, and a startup steam pipe 864 is installed on the pipe cap. Steam entering the pipe cap from the startup steam pipe is sprayed into the water inlet pipe through the porous pipe and then enters the heat exchange tube array to heat the equipment.
A second annular space is formed between the air cylinder 71 and the second cylinder 61 of the second housing, and air holes communicating the second annular space and the inner cavity of the air cylinder are formed in the air cylinder 71.
The second-stage conversion gas inlet pipe 81 is arranged on the second upper sealing head 62 and is communicated with an upper chamber 601 between the second upper sealing head 62 and the second inner upper sealing head 73, and the upper chamber 601 is communicated with a second annular gap.
An exhaust hole 631 is opened at the bottom of the second lower head 63, and the conversion gas exhaust pipe 821 is installed on the outer side edge of the exhaust hole 631 and extends downward in the vertical direction. A shift gas horizontal pipe 822, the outlet of which is formed as a shift gas outlet 823, is horizontally installed on the shift gas outlet pipe 821.
The conversion gas concentration pipe 82 is provided at the center of the gas cylinder 71 and extends in the vertical direction, and a through-hole-shaped gas hole communicating with the inner chamber of the gas cylinder is provided in the pipe wall of the conversion gas concentration pipe 82. The top end of the shift gas concentration tube 82 is closed and accommodated in the inner chamber of the gas cylinder 71, and the lower end of the shift gas concentration tube 82 extends downward and is connected to the inner edge of the exhaust hole 631 after penetrating the second inner lower seal 77.
Specifically, in this embodiment, a discharge pipe 78 is sleeved on the shift gas collecting pipe 82, the upper end of the discharge pipe 78 is connected to the lower tube plate 76, and the lower end of the discharge pipe 78 penetrates through the second lower inner seal head and is then sealingly mounted at the bottom of the second lower seal head 63. A discharge cavity 602 is formed between the second lower head 63 and the second inner lower head 77, i.e. a discharge cavity is provided at the bottom of the second housing.
A discharge hole 781 communicating with the discharge cavity 602 is formed in the discharge pipe 78, a discharge pipe 632 communicating with the discharge cavity 602 is mounted on the outer side of the second lower head 63 of the second housing, a circular discharge cavity 782 is formed between the discharge pipe 78 and the conversion gas collecting pipe 82, and the discharge cavity 782 is communicated with the inner cavity of the gas distribution cylinder. Catalyst in the inner cavity of the gas cylinder can enter the discharge cavity 602 after passing through the discharge cavity 782 and the discharge hole 781, and then is discharged from the discharge pipe 632.
A mounting hole 721 is formed in the center of the upper tube plate 72, the mounting hole 721 is used for inserting the shift gas concentration tube 82 into the gas cylinder 71, a sealing cover 74 is detachably mounted on the mounting hole 721, the sealing cover 74 comprises a flange 741 and a sealing cover 742 connected to the flange 741, the sealing cover 742 is in a downwardly protruding circular arc shape, and in the embodiment, the sealing cover 742 is made of a hemispherical cap.
A second upper manhole 621 is installed on the second upper head 62, and a second lower manhole 635 is installed on the second lower head 63.
In this embodiment, the connection portion 200 has a cylindrical shape extending in the vertical direction. And a support cylinder 400 is installed at the lower side of the second lower head 63 of the temperature-controlled reaction part 300, and the support cylinder 400 is used for installing the composite heat-insulating serial temperature-controlled converter device on a corresponding foundation.
Example 2
Referring to fig. 7, a shift process is performed by using the composite adiabatic serial temperature shift converter device described in embodiment 1, and in fig. 7, for clarity of illustration, the equipment nozzles of the composite adiabatic serial temperature shift converter device are disposed on the same drawing, and the specific flow of the shift process includes:
primary adiabatic conversion: the raw material gas 910 enters the refrigerant flow passage of the heat exchanger 430 to be heated, and the raw material gas discharged from the refrigerant flow passage of the heat exchanger 430 is split into two paths after detoxication, wherein one path is the feed gas, and the other path is the cold shock gas. The feed gas enters the gas inlet cavity 102 of the adiabatic reaction part 100 through the raw gas inlet pipe 32 along the feed pipe 432, flows upwards along the first annular gap into the gas distribution cavity 101, and enters the inner cavity of the inner cylinder through the top grid 23 for reaction. The cold shock gas enters the inner cavity of the inner cylinder through the cold shock gas inlet 351 along the cold shock pipeline 433, and is mixed with the feed gas to react. The raw material gas is reacted to produce a first-stage reformed gas, and the first-stage reformed gas is discharged from the first-stage reformed gas outlet pipe 31.
And (3) secondary temperature control conversion: the primary shift gas discharged from the adiabatic reaction part 100 enters the mixer 420 along the primary discharge pipe 421, and the adjustment steam and adjustment water 950 enter the mixer 420 to adjust the water-gas ratio and the temperature of the primary shift gas. In this embodiment, the conditioning steam is by-product steam described below, and the conditioning water is boiler water.
After the adjustment of the water-gas ratio and the temperature is completed, the first-stage conversion gas discharged from the mixer 420 enters the upper chamber 601 of the temperature control reaction part 300 through the second-stage conversion gas inlet pipe 81, then enters the inner cavity of the gas distribution cylinder through the second annular gap to react to generate the second-stage conversion gas 920, the second-stage conversion gas enters the heating medium flow passage of the heat exchanger 430 to heat the raw gas, and the second-stage conversion gas 920 discharged from the heat exchanger 430 enters the next process.
Saturated water in the steam drum 410 enters the water inlet pipe 86 through the water inlet 662, then enters the heat exchange tube 75, absorbs reaction heat to form a steam-water mixture, enters the steam-water mixture outlet pipe 85, and then returns to the steam drum 410 through the steam-water discharge pipe 851 to carry out byproduct steam.
The steam by-produced in the drum 410 is discharged through the main steam pipe 412 and is split into two streams, wherein one stream is discharged from the first steam branch 413 to form the external steam 940, and the other stream is introduced into the mixer 420 along the second steam branch 414 as conditioning steam for other process requirements.
The supplementary demineralized water 930 is introduced into the drum 410 through the demineralized water inlet pipe 411 for supplementing the amount of water in the drum.
In the embodiment, in the raw material gas, the volume ratio of dry CO is 65% and the water-gas ratio is 0.51; the inlet temperature of the feed gas and the cold shock gas entering the adiabatic reaction part is 257 ℃; in the adiabatic reaction section, the reaction pressure was 6.15MPaG; the outlet temperature of the first-stage conversion gas in the adiabatic reaction part is 431 ℃; the volume ratio of the dry-base CO of the first-stage converted gas is 31.4 percent, and the water-gas ratio of the first-stage converted gas after water supplementing is 0.61; the inlet temperature from the first-stage conversion gas to the temperature-control reaction part is 294 ℃; the outlet temperature of the two-stage conversion gas in the temperature-control reaction part is 325 ℃. The volume ratio of dry CO in the two-stage shift gas was 2.7%.
Wherein the volume ratio of COS in the two-stage conversion gas is 0.0014% dry basis and the volume ratio of methane is 0.038% dry basis.
In this example, the drum only produced a single vapor at a pressure of 6.7MpaG.
Claims (7)
1. The composite heat-insulating serial control temperature conversion furnace device is characterized by comprising a heat-insulating reaction part, a temperature control reaction part and a connecting part connected between the heat-insulating reaction part and the temperature control reaction part, wherein the heat-insulating reaction part is positioned above the temperature control reaction part;
the heat insulation reaction part comprises a first shell extending along the vertical direction, wherein the first shell is cylindrical, a first inner part is arranged in the first shell, and comprises an inner cylinder extending along the vertical direction, a first inner lower seal head hermetically arranged at the lower end of the inner cylinder and a top grid arranged at the upper end of the inner cylinder; an annular first annular gap is formed between the inner cylinder and the first shell, an air distribution cavity is formed between the top grille and the top of the first shell, and an air inlet cavity is formed between the first inner lower seal head and the bottom of the first shell; the upper end and the lower end of the first annular gap are respectively communicated with the air distribution cavity and the air inlet cavity; the first inner piece is supported at the bottom of the first shell, and the first inner piece is in sliding connection with the inner peripheral wall of the first shell, so that the first inner piece can freely stretch and retract in the vertical direction;
the first shell is provided with a cold shock air pipe, and the outlet end of the cold shock air pipe is positioned in the inner cavity of the inner cylinder;
a raw gas inlet pipe and a section of conversion gas outlet pipe are arranged at the bottom of the first shell, wherein the raw gas inlet pipe is communicated with the gas inlet cavity, one end of the section of conversion gas outlet pipe is communicated with the inner cavity of the inner cylinder, and the other end of the section of conversion gas outlet pipe extends downwards out of the first shell;
the temperature control reaction part comprises a second shell extending along the vertical direction, the second shell is cylindrical, a second internal part is arranged in the second shell, the second internal part comprises an air distribution cylinder extending along the vertical direction, an upper tube plate arranged at the upper end of the air distribution cylinder, a lower tube plate arranged at the lower end of the air distribution cylinder, and a heat exchange tube array is arranged between the upper tube plate and the lower tube plate; a second annular gap is formed between the air distribution cylinder and the second housing, and an air distribution hole which is communicated with the second annular gap and the inner cavity of the air distribution cylinder is formed in the air distribution cylinder;
a steam-water mixture outlet pipe and a two-section conversion gas inlet pipe are arranged at the top of the second shell, a water inlet pipe is arranged at the bottom of the second shell, the upper end of the heat exchange tube array is communicated with the steam-water mixture outlet pipe, and the lower end of the heat exchange tube array is communicated with the water inlet pipe; the second-stage conversion gas inlet pipe is communicated with the second annular gap;
a conversion gas discharge pipe is arranged at the bottom of the second shell, a conversion gas concentration pipe is arranged at the central part of the gas cylinder and extends along the vertical direction, the top end of the conversion gas concentration pipe is accommodated in the inner cavity of the gas cylinder, and the lower end of the conversion gas concentration pipe extends downwards and is communicated with the conversion gas discharge pipe; the tube wall of the conversion gas concentration tube is provided with a through hole-shaped air hole communicated with the inner cavity of the gas distribution tube;
two layers of catalyst support plates are arranged in the inner cylinder along the height direction, namely a first catalyst support plate and a second catalyst support plate, wherein the first catalyst support plate is positioned above the second catalyst support plate, and an intermediate grille is arranged between the first catalyst support plate and the second catalyst support plate; a first catalyst cavity is formed in front of the first catalyst support plate and the top grid, a second catalyst cavity is formed between the middle grid and the second catalyst support plate, a cold shock cavity is formed between the first catalyst support plate and the middle grid, and the outlet end of the cold shock air pipe is positioned in the cold shock cavity; the first catalyst cavity and the second catalyst cavity are filled with catalyst, and no catalyst is filled in the cold shock cavity; the heat-insulating reaction part is sequentially provided with a first catalyst cavity, a cold shock cavity and a second catalyst cavity, wherein the cold shock cavity is used as a cold shock gas distribution cavity;
the cold shock air pipe and the inner cylinder are coaxially arranged, the inlet end of the cold shock air pipe extends out of the top of the first shell upwards, and the outlet end of the cold shock air pipe freely penetrates through the top grid and the first catalyst supporting plate downwards and then enters the cold shock cavity.
2. The shift converter device according to claim 1, wherein,
a discharge pipe is sleeved on the conversion gas concentration pipe, the upper end of the discharge pipe is connected to the lower pipe plate, and the lower end of the discharge pipe is hermetically arranged at the bottom of the second shell; a discharging cavity is arranged at the bottom of the second shell, a discharging hole communicated with the discharging cavity is formed in the discharging pipe, a discharging pipe communicated with the discharging cavity is arranged at the outer side of the second shell, a circular discharging cavity is formed between the discharging pipe and the conversion gas collecting pipe, and the discharging cavity is communicated with the inner cavity of the gas distribution cylinder.
3. The shift converter device according to claim 1, wherein,
a mounting hole is formed in the center of the upper tube plate and used for inserting the conversion gas concentration tube into the gas distribution cylinder, a sealing cover is detachably mounted on the mounting hole and comprises a flange and a sealing cover connected to the flange, and the sealing cover is in a downward protruding arc shape.
4. A shift process using the composite adiabatic series control temperature shift converter device according to any one of claims 1 to 3, comprising:
primary adiabatic conversion: the raw gas is detoxified after passing through the heat exchanger, the detoxified raw gas is divided into two paths, one path is feed gas, the other path is cold shock gas, the feed gas enters the air inlet cavity of the adiabatic reaction part through the raw gas inlet pipe, then flows upwards along the first annular gap to enter the air distribution cavity, and then enters the inner cavity of the inner cylinder through the top grid to react; cold shock gas enters the inner cavity of the inner cylinder through a cold shock gas pipe, and is mixed with feed gas to react; the raw material gas is reacted to generate a first-stage conversion gas, and the first-stage conversion gas is discharged from a first-stage conversion gas outlet pipe;
and (3) secondary temperature control conversion: the first-stage conversion gas enters the mixer, the adjusting steam and adjusting water enter the mixer to adjust the water-gas ratio and the temperature of the first-stage conversion gas, the first-stage conversion gas discharged from the mixer enters the temperature control reaction part through the second-stage conversion gas inlet pipe, then enters the inner cavity of the gas distribution cylinder through the second annular gap to react to generate the second-stage conversion gas, and the second-stage conversion gas enters the conversion gas concentration pipe and then is discharged through the conversion gas discharge pipe; the two-stage converter enters a heat exchanger to heat the raw material gas;
saturated water in the steam drum enters the heat exchange tube by the water inlet pipe, exchanges heat and then is discharged by the steam-water mixture outlet pipe to enter the steam drum to produce byproduct steam.
5. The shift process as claimed in claim 4, wherein,
the byproduct steam of the steam drum is used as conditioning steam.
6. The shift process according to claim 4, wherein,
in the raw material gas, the volume ratio of dry CO is 62-75% and the water-gas ratio is 0.48-0.54;
the inlet temperature of the feed gas and the cold shock gas entering the adiabatic reaction part is 250-260 ℃;
in the adiabatic reaction part, the reaction pressure is 6.0-6.2MPaG;
the outlet temperature of the first-stage conversion gas in the adiabatic reaction part is 430-435 ℃;
the volume ratio of the dry basis CO of the one-stage converted gas is 31-37%,
after the water is supplemented to the first-stage converted gas, the water-gas ratio is 0.58-0.66;
the inlet temperature from the first-stage conversion gas to the temperature-control reaction part is 290-298 ℃;
the outlet temperature of the second-stage conversion gas in the temperature-control reaction part is 315-330 ℃;
the volume ratio of dry-base CO in the two-stage conversion gas is 2.5-3.5%;
the pressure of the byproduct steam in the steam drum is 6.3-6.9MPaG.
7. The shift process as claimed in claim 4, wherein,
the drum produces only one type of steam.
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