CN212237215U - Self-heating purifying furnace and shift reaction and heat recovery device - Google Patents
Self-heating purifying furnace and shift reaction and heat recovery device Download PDFInfo
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- CN212237215U CN212237215U CN202020139745.7U CN202020139745U CN212237215U CN 212237215 U CN212237215 U CN 212237215U CN 202020139745 U CN202020139745 U CN 202020139745U CN 212237215 U CN212237215 U CN 212237215U
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Abstract
The utility model relates to an auto-heating purification furnace and transformation reaction and heat recovery device. The device comprises a closed furnace body, a middle partition plate, a catalyst frame and a central tube, wherein the closed furnace body consists of a cylinder body, an upper end socket arranged at the upper end of the cylinder body, and a lower end socket arranged at the lower end of the cylinder body; the lower end enclosure is provided with a process gas outlet; the middle partition plate is arranged in the closed furnace body and divides the furnace body into an upper section and a lower section; the upper section of the furnace body is provided with a catalyst frame and a central pipe, and the catalyst frame is provided with a hole; the upper end of the central tube is connected with a feed gas inlet of an upper end socket of the furnace body, a small hole is formed in the middle of the central tube to collect gas, the lower end of the central tube penetrates through the middle partition plate, and a shift catalyst is filled between the central tube at the upper section of the self-heating purification furnace and the catalyst frame. The method is divided into a reaction section and a purification section, and high-temperature gas generated by the shift reaction of one part of raw material gas is mixed with the other part of raw material gas for purification.
Description
Technical Field
The utility model belongs to the field of chemical equipment, in particular to an auto-heating purification furnace.
Background
CO shift (CO + H)2O→H2+CO2) Means that the raw material gas passes through a catalyst in a reactor under certain temperature and pressure to lead CO and H in the raw material gas2O reacts to generate H2And CO2So as to achieve the purpose of adjusting the proportion of the carbon monoxide and the hydrogen, and the carbon monoxide conversion process is an indispensable important process in the modern coal chemical industry.
Along with the rapid development of coal chemical industry in China, entrained flow bed gasification technologies represented by coal water slurry pressure gasification and dry pulverized coal pressure gasification are increasingly applied. The raw gas sent to the conversion by the entrained flow bed pressurized gasification has the characteristics of high CO content, high water-gas ratio, high dew point temperature and high ammonia content, and the CO dry basis volume content in the raw gas generated by the pressurized gasification of the common coal water slurry can reach more than 45 percent, and the water-gas ratio can reach 1.2-1.4; the dry-basis volume content of CO in the dry pulverized coal pressurized gasification raw material gas reaches 60-70 percent, and the water-gas ratio reaches-1.0. Therefore, in the process of raw gas conversion, not only the CO conversion reaction generates a large amount of heat, but also more residual steam in the conversion gas is generated, so that a large amount of heat needs to be recovered, a large amount of condensate needs to be separated, and the conversion gas is sent to a lower working section and ammonia needs to be washed out so as to avoid influencing the lower working section. The traditional conversion process adopts an adiabatic conversion furnace, conversion needs to be divided into multiple stages to obtain higher conversion rate, but the reaction temperature of the first stage of the conversion is easy to exceed the temperature due to high CO content. The water heat transfer type isothermal shift reactor (also called isothermal shift converter or temperature control shift converter) developed in recent years can remove the reaction heat in time, and solves the problem of overhigh reaction temperature.
The isothermal shift process or isothermal and adiabatic combined process is characterized in that crude gas is subjected to heat exchange with shift gas to raise the temperature, then the crude gas is subjected to shift reaction in an isothermal shift furnace, most of heat generated by the shift reaction is removed through byproduct steam, the shift gas discharged from the shift furnace is subjected to byproduct low-pressure steam in a steam generator and low-temperature desalted water heated by a desalted water heater to recover the waste heat of shift gas, the shift gas is cooled by circulating water through a water cooler to be shifted, and finally NH in the shift gas is washed out through an ammonia washing tower3(ii) a Condensate is generated in each step in the process of recovering the waste heat of the conversion gas and cooling, and the condensate needs to be separated by an independent separator; in actual operation, because the outlet temperature of the isothermal converter is lower and the temperature difference with the crude gas is small, the crude gas is difficult to be treated by adopting a heat exchange methodThe temperature of the coal gas is increased to the temperature required by the reaction.
The isothermal shift system for removing CO in the raw material gas disclosed in the Chinese invention patent application with the application number of 201520522410.2 and the hydrothermal shift process for energy-saving deep conversion of high-grade steam as a byproduct disclosed in the Chinese invention patent application with the application number of 201210185731.9 both adopt a hydrothermal shift type isothermal shift furnace to control the reaction temperature, the crude gas is heated by a heat exchanger, and the catalyst needs to increase the temperature of the raw material gas at the later stage in actual operation because the temperature difference of heat exchange is small and the heat exchange area is required to be very large; moreover, dust contained in the feed gas is easy to block the heat exchanger, and the long-period stable operation of the conversion unit is influenced; condensate generated in the conversion gas waste heat recovery and cooling process is separated by adopting an independent gas-liquid separator, and ammonia in the conversion gas is washed by an ammonia washing tower, so that the equipment has multiple processes, the piping is complex, and the system cost is high.
Disclosure of Invention
To prior art not enough, the utility model aims to provide an autothermic purification stove, it can realize dividing into two strands with the feed gas, and the one carries out shift reaction, then mixes with another strand feed gas, makes the feed gas reach the required reaction temperature of reaction, fully satisfies the requirement that the catalyst later stage raised the temperature.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
the self-heating purification furnace comprises a closed furnace body, a middle partition plate, a catalyst frame and a central tube, wherein the closed furnace body consists of a cylinder body, an upper end enclosure arranged at the upper end of the cylinder body, and a lower end enclosure arranged at the lower end of the cylinder body; the lower end enclosure is provided with a process gas outlet; the middle partition board is arranged in the closed furnace body and divides the furnace body into an upper section and a lower section; the upper section of the furnace body is provided with a catalyst frame and a central pipe, and the catalyst frame is provided with a hole; the upper end of the central tube is connected with a feed gas inlet of an upper end enclosure of the furnace body, the middle part of the central tube is provided with a hole for collecting gas, the lower end of the central tube penetrates through the middle partition plate, and a shift catalyst is filled between the central tube at the upper section of the self-heating purification furnace and the catalyst frame. The raw material gas entering the upper section of the furnace body enters the catalyst bed layer through the holes on the catalyst frame for conversion reaction, the reacted process gas enters the central tube through the small holes of the central tube, is fully mixed with the unheated raw material gas entering the central tube from the raw material gas inlet, enters the lower section of the self-heating purification furnace, is purified by the purifying agent bed layer, and then leaves the self-heating purification furnace from the process gas outlet.
According to the scheme, the shift catalyst is preferably a sulfur-tolerant shift catalyst.
According to the scheme, preferably, the second raw material gas inlet is positioned on the axis of the upper end socket of the furnace body.
According to the scheme, the lower end of the central pipe penetrates through the middle partition plate and then is connected with the gas redistributor.
According to the scheme, the catalyst frame is a cylinder coaxial with the furnace body, and the lower end of the catalyst frame is fixed on the middle partition plate.
According to the scheme, a gap is formed between the furnace wall of the self-heating purification furnace and the catalyst frame, so that the furnace wall is protected from over-temperature.
According to the scheme, the inert ceramic balls are filled in the lower end socket at the bottom of the furnace body to support the catalyst, and the inert ceramic balls are favorable for uniform distribution of gas.
According to the scheme, the bottom of the middle partition plate is provided with inert ceramic balls for supporting the catalyst;
according to the scheme, the shift catalyst filled in the catalyst frame is preferably a sulfur-resistant shift catalyst.
According to the scheme, the lower section of the autothermal purification furnace is filled with the purifying agent.
The shift reaction and heat recovery device comprises a raw material gas separator, a raw material gas preheater, an autothermal purification furnace, a temperature-controlled shift converter, a steam generator, a desalted water heater and a shift gas water cooler; the method comprises the steps that after condensate is separated from raw material gas through a raw material gas separator, an outlet of the raw material gas separator is provided with two branch pipes, outlet gas is divided into two strands, one strand of outlet gas is connected with a second raw material gas inlet of an autothermal purification furnace and enters a central pipe, the other strand of outlet gas is connected with a raw material gas preheater, an outlet of the raw material gas preheater is connected with a first raw material gas inlet of the autothermal purification furnace, conversion reaction is carried out at the upper section of the autothermal purification furnace, high-temperature gas after reaction enters the central pipe and is mixed with unreacted raw material gas to enter the lower section of the autothermal purification furnace for purification, an outlet of the autothermal purification furnace is connected with an inlet of a temperature-control conversion furnace, an outlet of the temperature-control conversion.
According to the scheme, the shift reaction and heat recovery device further comprises a steam drum for collecting steam generated by the temperature-controlled shift converter.
According to the scheme, the number of the temperature control shift converters is one or more, and the temperature control shift converters are connected in sequence.
According to the scheme, the number of the steam generators can be multiple, and the steam generators comprise a low-pressure steam generator and a secondary low-pressure steam generator.
According to the scheme, the steam generator is a vertical steam generator, and the steam generator and the desalted water heater are integrated with a liquid separator.
According to the scheme, the gas-water cooler of the shift converter is integrated with a liquid separator and an ammonia washing tower.
The utility model discloses following beneficial effect has:
the utility model discloses an autogenous heat purifies the stove and falls into the reaction section with self-heating purification stove and purifies the section, the high-temperature gas that produces of shift reaction through some feed gas mixes with another part feed gas, make the feed gas reach the required reaction temperature of reaction and can purify as required, can fully satisfy the requirement that the temperature was carried in the catalyst later stage, avoided using the heat exchange can't satisfy the requirement of adjusting the temperature of advancing the shift converter, shift converter import temperature control is freely, can fully satisfy the requirement that the temperature was carried in the catalyst later stage.
The primary or secondary temperature-control shift converter can be selected according to the requirement, the requirement of reaction conversion rate is met, the reaction temperature is controllable, and the problem of over-temperature of the catalyst bed layer is solved;
the vertical steam generator and the desalted water heater which are integrated with the liquid separator are used, and the liquid separator and the water cooler of the ammonia washing tower are integrated, so that the conversion gas waste heat recovery efficiency is improved, the equipment is reduced, and the process is shortened; the system has the advantages of low temperature of the whole system, high safety, sufficient heat recovery, short flow, small system resistance, small occupied area, low manufacturing cost, equipment investment saving, occupied area and the like.
Drawings
FIG. 1 is a diagram of an autothermal reformer installation. In the figure: the device comprises an A01 upper end socket, an A02 cylinder, an A03 lower end socket, an A04 middle partition plate, an A05 catalyst frame, an A06 central tube, an A07 first raw material gas inlet, an A08 second raw material gas inlet, an A09 process gas outlet and an A10 gas redistributor.
Fig. 2 is a schematic view of the shift reaction and heat recovery device and the process flow thereof in embodiment 1 of the present invention. In the figure: the system comprises a replacement gas separator 1, a gas preheater 2, a self-heating purification furnace 3, a temperature control shift converter 4, a steam drum 5, a low-pressure steam generator 6, a secondary low-pressure steam generator 7, a desalted water heater 8 and a shift gas water cooler 9.
Fig. 3 is a schematic view of the shift reaction and heat recovery device and the process thereof in embodiment 2 of the present invention. In the figure: the system comprises a replacement gas separator 1, a gas preheater 2, a self-heating purification furnace 3, a first temperature-control shift converter 4, a first steam pocket 5, a second temperature-control shift converter 5, a second steam pocket 7, a low-pressure steam generator 8, a desalted water heater 9 and a shift gas water cooler 10.
Detailed Description
The invention will be further explained with reference to the drawings:
referring to fig. 1, the self-heating purification furnace is constructed as follows:
the device comprises a closed furnace body consisting of a cylinder A02, an upper end enclosure A01 arranged at the upper end of the cylinder and a lower end enclosure A03 arranged at the lower end of the cylinder, a middle partition plate A04, a catalyst frame A05 and a central tube A06, wherein the upper end enclosure A01 of the furnace body is provided with a first raw material gas inlet A07 and a second raw material gas inlet A08; the furnace body lower end socket A03 is provided with a process gas outlet A09; the middle partition plate A04 is arranged in the closed furnace body and divides the furnace body into an upper section and a lower section; the upper section of the furnace body is provided with a catalyst frame A05 and a central tube A06, the upper end of the central tube A06 is connected with a raw material gas inlet A08 on the axis of the upper end socket of the furnace body, the middle part of the central tube is provided with a small hole for collecting gas after catalytic conversion reaction of the catalyst in the catalytic frame, and the lower end of the central tube penetrates through a middle partition plate and is connected with a gas redistributor A10; the catalyst frame A05 is coaxial with the furnace body, the lower end of the catalyst frame A05 is welded on the middle partition plate, and a small hole is formed in the catalyst frame; the raw material gas entering the upper section of the furnace body enters the catalyst bed layer for conversion reaction after being uniformly distributed through the small holes on the catalyst frame, the process gas after reaction enters the central tube through the small holes of the central tube, is fully mixed with unheated raw gas entering the central tube A06 through the second raw material gas inlet A08, enters the purifying agent bed layer at the lower section of the self-heating purifying furnace through the distribution of the gas redistributor A10, and then leaves the self-heating purifying furnace from the process gas outlet A09 after being purified.
The catalyst frame at the upper section of the self-heating purification furnace is filled with a shift catalyst, the lower section of the self-heating purification furnace is filled with a purifying agent, and the lower seal head A03 is filled with inert ceramic balls which are used as a support catalyst and are beneficial to the uniform distribution of gas.
The working principle is as follows: a small amount of raw material gas (accounting for 10-30% of the total amount, and further 15-25%) heated by the gas preheater enters a gap between the furnace wall of the furnace body and the catalyst frame A05 from the first raw material gas inlet A07, enters the upper catalyst bed layer of the autothermal purification furnace after being uniformly distributed by the catalyst frame A05, is subjected to shift reaction under the action of a shift catalyst in the catalyst frame, high-temperature process gas after reaction enters the central tube through small holes in the central tube A06, is fully mixed with unheated raw gas entering the central tube A06 from the second raw material gas inlet A08 to meet the inlet temperature requirement of the autothermal purification furnace, enters the lower purifier bed layer of the autothermal purification furnace after being uniformly distributed by the gas redistributor A12, and then leaves the autothermal purification furnace from the process gas outlet A09.
Referring to fig. 2 and 3, the shift reaction and heat recovery device provided by the invention comprises a raw material gas separator, a raw material gas preheater, an autothermal purification furnace, a temperature-controlled shift converter, a steam generator, a desalted water heater and a shift gas water cooler; the method comprises the steps that after condensate is separated from raw material gas through a raw material gas separator, an outlet of the raw material gas separator is provided with two branch pipes, outlet gas is divided into two strands, one strand of outlet gas is connected with a second raw material gas inlet of an autothermal purification furnace and enters a central pipe, the other strand of outlet gas is connected with a raw material gas preheater, an outlet of the raw material gas preheater is connected with a first raw material gas inlet of the autothermal purification furnace, conversion reaction is carried out at the upper section of the autothermal purification furnace, high-temperature gas after reaction enters the central pipe and is mixed with unreacted raw material gas to enter the lower section of the autothermal purification furnace for purification, an outlet of the autothermal purification furnace is connected with an inlet of a temperature-control conversion furnace, an outlet of the temperature-control conversion.
Furthermore, the shift reaction and heat recovery device also comprises a steam drum for collecting steam generated by the temperature-controlled shift converter.
The number of the temperature control change furnaces is one or more, and the temperature control change furnaces are connected in sequence.
The steam generator can be a plurality of steam generators, including a low-pressure steam generator and a secondary low-pressure steam generator.
The vertical steam generator and the desalted water heater can be integrated with a liquid distributor.
The water cooler can be integrated with a liquid separator and an ammonia washing tower.
The present invention will be further described with reference to the following examples.
Example 1
As shown in figure 2, the raw gas (pressure 6.3MPaG, temperature 240 ℃) from the coal water slurry gasification device is separated into two strands after liquid water is separated by a raw material gas separator 1, wherein one strand of the raw gas is heated to 260 ℃ by a raw material gas preheater 2 and then enters the upper section of a self-heating purification furnace 3, after reaction, the raw gas is fully mixed with the other strand of the raw gas (about 75%) which directly enters a central pipe, the temperature is about 275 ℃ to remove dust and toxic substances from the lower section of the self-heating purification furnace, and then the raw gas is subjected to shift reaction by a temperature-controlled shift furnace 4. Under the action of the shift catalyst between tubes, CO and H in the raw gas entering the shift converter with controlled temperature2And (3) carrying out shift reaction on the O, discharging a large amount of reaction heat through the shift reaction, carrying out heat exchange with boiler feed water in the pipe to obtain a byproduct of 4.5MPa steam, and feeding the byproduct of steam into a steam drum 5 to separate water and then feeding the steam into a steam pipe network. The temperature of the transformed gas discharged from the temperature-controlled shift converter is 270 ℃, the CO content is less than or equal to 3.0 percent (dry basis, mol percent) and the un-transformed gas are mixedThen, the steam enters the low-pressure steam generator 6 to produce a byproduct of 1.5MPa steam, the process temperature is reduced to 200 ℃, the condensate is separated by the liquid separator integrated at the lower part, the steam enters the secondary low-pressure steam generator 7 to produce a byproduct of 0.5MPa steam, the process temperature is reduced to 160 ℃, the condensate is separated by the liquid separator integrated at the lower part, and the condensate enters the desalted water heater 8. The process gas at the outlet of the desalted water heater 8 is separated into condensate through the liquid separator integrated at the lower part and then enters the water cooler 9 of the shift gas, the temperature of the process gas is reduced to 40 ℃, the condensate is separated through the liquid separator integrated at the lower part, and the process gas is subjected to ammonia washing and then goes to the post-process.
Example 2
As shown in figure 3, the raw gas (pressure 6.0MPaG, temperature 232 ℃) from the coal water slurry gasification device is separated into two strands after liquid water is separated by a raw material gas separator 1, wherein one strand of the raw gas with the concentration of about 12% is heated to 260 ℃ by a raw material gas preheater 2 and then enters the upper section of a self-heating purification furnace 3, after reaction, the raw gas with the concentration of about 88% is mixed by a central pipe, then the temperature is about 265 ℃ and the mixture is sent to the lower section of the self-heating purification furnace 3 to remove dust and toxic substances, and then the raw gas is subjected to shift reaction by a first-stage temperature. Under the action of the shift catalyst between tubes, CO and H in the raw gas entering the shift converter with controlled temperature2And (3) carrying out shift reaction on the O, discharging a large amount of reaction heat through the shift reaction, generating a byproduct of 4.5MPa steam after water supply and heat exchange of the boiler in the pipe, and sending the byproduct of steam into a steam pipe network after the steam enters a first steam drum 5 to separate water. The temperature of the transformed gas which is discharged from the first-stage temperature-controlled shift converter is 270 ℃, the CO content is less than or equal to 3.5 percent (dry basis, mol percent), and the transformed gas enters a second-stage temperature-controlled shift converter 6 for continuous shift reaction. The shift gas entering the second-stage temperature-control shift converter 5 is CO and H under the action of the inter-tube shift catalyst2And (3) carrying out shift reaction on the O, wherein the reaction heat released by the shift reaction is subjected to water supply and heat exchange in the boiler in the pipe to obtain a byproduct of 1.0MPa steam, and the byproduct of steam enters a second steam pocket 7 to separate water and then is sent into a steam pipe network. The temperature of the shifted air which is discharged from the second-stage temperature-control shift converter is 210 ℃, the CO content is less than or equal to 0.6 percent (dry basis, mol percent), the shifted air firstly enters a low-pressure steam generator 8 to produce 0.5MPa of steam as a byproduct, the temperature of the process air is reduced to 160 ℃, condensate is separated by a liquid separator integrated at the lower part, and then the condensate enters a desalted water heater 9. The process gas at the outlet of the desalted water heater 9 is separated from condensate by a liquid separator integrated at the lower part and then enters a water cooler 10 of the conversion gasThe process temperature is reduced to 40 ℃, condensate is separated by a liquid separator integrated at the lower part, and ammonia is washed and then the condensate is sent to the post-process.
Claims (10)
1. The self-heating purification furnace comprises a closed furnace body, a middle partition plate, a catalyst frame and a central tube, wherein the closed furnace body consists of a cylinder body, an upper end enclosure arranged at the upper end of the cylinder body, and a lower end enclosure arranged at the lower end of the cylinder body; the lower end enclosure is provided with a process gas outlet; the middle partition board is arranged in the closed furnace body and divides the furnace body into an upper section and a lower section; the upper section of the furnace body is provided with a catalyst frame and a central pipe, and the catalyst frame is provided with a hole; the upper end of the central tube is connected with a second raw material gas inlet of an upper end enclosure of the furnace body, a small hole is formed in the middle of the central tube to collect gas, the lower end of the central tube penetrates through the middle partition plate, and a shift catalyst is filled between the central tube at the upper section of the self-heating purification furnace and the catalyst frame.
2. The autothermal purifier of claim 1, wherein: and the second raw material gas inlet is positioned on the axis of the upper seal head of the furnace body.
3. The autothermal purifier of claim 1, wherein: the lower end of the central tube penetrates through the middle partition plate and then is connected with the gas redistributor.
4. The autothermal purifier of claim 1, wherein: the catalyst frame is a cylinder coaxial with the furnace body, and the lower end of the catalyst frame is fixed on the middle partition plate.
5. The autothermal purifier of claim 1, wherein: a gap is formed between the furnace wall of the self-heating purification furnace and the catalyst frame, so that the furnace wall is protected from over-temperature.
6. The autothermal purifier of claim 1, wherein: inert ceramic balls are filled in the lower end socket at the bottom of the furnace body and used for supporting the catalyst; and the bottom of the middle partition plate is provided with inert ceramic balls for supporting the catalyst.
7. The autothermal purifier of claim 1, wherein: the conversion catalyst filled in the catalyst frame is a sulfur-resistant conversion catalyst; the lower section of the self-heating purification furnace is provided with a purifying agent.
8. Shift reaction and heat recovery device, its characterized in that: comprises a raw material gas separator, a raw material gas preheater, the self-heating purification furnace of claim 1, a temperature-controlled shift converter, a steam generator, a desalted water heater and a shift gas water cooler; the method comprises the steps that after condensate is separated from raw material gas through a raw material gas separator, an outlet of the raw material gas separator is provided with two branch pipes, outlet gas is divided into two strands, one strand of outlet gas is connected with a second raw material gas inlet of an autothermal purification furnace and enters a central pipe, the other strand of outlet gas is connected with a raw material gas preheater, an outlet of the raw material gas preheater is connected with a first raw material gas inlet of the autothermal purification furnace, conversion reaction is carried out at the upper section of the autothermal purification furnace, high-temperature gas after reaction enters the central pipe and is mixed with unreacted raw material gas to enter the lower section of the autothermal purification furnace for purification, an outlet of the autothermal purification furnace is connected with an inlet of a temperature-control conversion furnace, an outlet of the temperature-control conversion.
9. The shift reaction and heat recovery device according to claim 8, wherein: the number of the temperature control shift converters is one or two, and the temperature control shift converters are connected in sequence; the steam generators are multiple and comprise a low-pressure steam generator and a secondary low-pressure steam generator; the shift reaction and heat recovery device also comprises a steam drum for collecting steam generated by the temperature-controlled shift converter.
10. The shift reaction and heat recovery device according to claim 8, wherein: the steam generator and the desalted water heater are integrated with a liquid separator; the shift gas water cooler is integrated with a liquid separator and an ammonia washing tower.
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