CN113460961B - Sleeve type controllable semi-isothermal shift converter - Google Patents
Sleeve type controllable semi-isothermal shift converter Download PDFInfo
- Publication number
- CN113460961B CN113460961B CN202110763334.4A CN202110763334A CN113460961B CN 113460961 B CN113460961 B CN 113460961B CN 202110763334 A CN202110763334 A CN 202110763334A CN 113460961 B CN113460961 B CN 113460961B
- Authority
- CN
- China
- Prior art keywords
- furnace body
- gas
- boiler water
- cylinder body
- central tube
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
- C01B2203/0883—Methods of cooling by indirect heat exchange
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to a sleeve type controllable semi-isothermal shift converter, which comprises a vertically extending cylindrical furnace body, wherein a coarse synthetic gas inlet is formed in the top of the furnace body, a shift gas outlet is formed in the bottom of the furnace body, a partition plate capable of dividing an inner cavity of the furnace body into an upper section and a lower section which are relatively independent is arranged in the furnace body, and the furnace further comprises an inner upper cylinder body, a central pipe, a boiler water inlet cavity, a steam collecting cavity, a boiler water column pipe, a sleeve, a steam drum and an inner lower cylinder body. According to the invention, through a sectional reaction technology, gas entering a bypass does not need to be independently heated to the activation temperature, the activation temperature can be achieved through a method of mixing the gas with the change gas at the upper section outlet of the change furnace, and the complexity of a process and equipment investment are reduced; a semi-isothermal zone is formed in the upper section by combining a controllable steam generation system, and the temperature of a conversion gas outlet can be effectively regulated by controlling the bypass air inflow and the boiler water flow according to the load of the crude synthetic gas or the water-gas ratio and the initial and final stage working conditions of the conversion catalyst, so that the stability of a downstream heat exchange system is ensured.
Description
Technical Field
The invention relates to a sleeve type controllable semi-isothermal shift converter.
Background
China is a country with rich coal resources and relatively lacking petroleum resources, and enters the 21 st century, and the coal chemical industry of China enters the rapid development stage. Coal gasification is an important method for chemical processing of coal and is a key for realizing clean utilization of coal.
The CO conversion process is an indispensable ring in the modern coal chemical technology and plays a role in supporting the rising and falling. The purpose of the CO shift is to adjust H in the synthesis gas 2 And CO concentration, meeting the demands of downstream users. Depending on the nature of the CO reaction as a strongly exothermic reaction, there are currently generally several types of reactors:
(1) An axial reactor. The inside of the axial reactor is filled with catalyst, and the shift gas passes through the catalyst bed layer from the axial direction to carry out adiabatic shift reaction. The reactor has the characteristics of simple structure and large catalyst loading. However, since the whole shift gas needs to pass through the whole catalyst bed, the pressure drop of the shift gas is large, especially in the case of the last stage of catalyst crushing, the pressure drop caused by the shift furnace is large, and the pressure drop of the whole shift system is increased. In the case of a medium water gas ratio, high CO crude synthesis gas reaction, excessive temperatures are extremely likely to result. Therefore, the axial reactor is only suitable for places with small adiabatic temperature rise such as low-temperature transformation.
(2) An axial radial reactor. Unlike the axial reactor, the flow direction of the shift gas of the axial-radial reactor is along the radial direction of the reactor, from outside to inside, through the catalyst bed, into the central tube and out of the reactor. The gas distribution of the reactor is stable, the gas distribution is not influenced by the filling density of the catalyst, and the bed pressure drop is small; compared with an axial shift furnace with the same working condition, the temperature of the cylinder body is lower, the diameter and the wall thickness of equipment are small, and the equipment investment is low; a catalyst with high activity and small particles can be selected; the outlet CO content is low.
(3) An isothermal reactor. The two shift converters adopt adiabatic reactors, and the shift reaction belongs to a strong exothermic reaction and is a thermodynamically controlled process, so that the shift process adopts a multi-stage and multi-time heat exchange reaction mode in the process setting. Thus, a series of problems of relatively complex technology, high heat loss, high steam consumption, high equipment cost and the like of the traditional technology are caused.
The isothermal reactor can immediately remove the reaction heat through a physical method of 'water heat removal', so that the catalyst bed can be maintained to operate at a stable low temperature, and a high CO conversion rate is ensured. The advantages of isothermal transformation techniques over traditional adiabatic transformations are as follows:
a. the isothermal transformation removes the reaction heat immediately, and the catalyst bed layer is maintained to run stably at a lower temperature;
b. the byproduct steam greatly reduces the energy consumption;
c. and the process flow reduces the pressure drop of the system and the investment of the device.
However, the isothermal transformation technology applied at present has the following problems:
(1) the byproduct steam in the isothermal shift furnace steam drum is saturated steam, and can not produce higher-quality superheated steam. The conversion device is a steam surplus device, and usually redundant steam is supplied to other users in the whole plant through a steam pipe network, and condensate is easy to generate when the saturated steam temperature is reduced, so that the steam cannot enter the pipe network. The outlet temperature of the traditional adiabatic shift converter is higher, usually more than 400 ℃, saturated steam can be overheated, and the isothermal shift converter is mostly taken away by a water circulation system due to the heat of reaction, the outlet temperature is only about 300 ℃, a superheated source cannot be provided, and the complexity and equipment investment of the process can be increased only by independently arranging a heating furnace or carrying out heat combination with other devices.
(2) The isothermal shift furnace temperature is difficult to adjust. The temperature of the outlet of the shift converter needs to be regulated frequently due to the influence of factors such as upstream load fluctuation, water-gas ratio fluctuation, catalyst end-stage temperature rising and the like. The water circulation between the steam drum and the heat exchange tube is natural circulation, namely, the steam circulation formed by the driving force generated by the density difference of the two-phase flow in the static pressure head of water and the heat exchange tube is utilized, so that the control of removing the reaction heat has a certain difficulty.
Disclosure of Invention
Aiming at the current state of the art, the invention provides the sleeve type sectional controllable semi-isothermal shift furnace which can meet the requirements of the crude synthesis gas shift reaction under the working conditions of different loads and water-gas ratio by sectional feeding and can adjust the temperature of the outlet shift gas to meet the requirements of the byproduct steam grade of a shift unit.
The technical scheme adopted for solving the technical problems is as follows:
the utility model provides a controllable semi-isothermal shift converter of bushing type, includes vertical extension and is cylindric furnace body, and open at this furnace body top has thick synthetic gas import, bottom to open has the transform gas export, be provided with the baffle that can separate its inner chamber into relatively independent upper segment and hypomere in the furnace body, controllable semi-isothermal shift converter of bushing type still includes:
an inner upper cylinder body is arranged in the upper section of the furnace body and is provided with an inner cavity for filling a heat insulation conversion reaction catalyst, an air inlet annular gap is formed between the outer peripheral wall of the inner upper cylinder body and the inner peripheral wall of the furnace body, and a plurality of first air inlets which are arranged at intervals are formed on the outer peripheral wall of the inner upper cylinder body;
the central tube is arranged at the central part of the inner upper cylinder body, the upper end of the central tube is closed, the lower end of the central tube is provided with a lower port communicated with the lower part of the partition plate, and the peripheral wall of the central tube is provided with a plurality of air vents for allowing the gas in the inner upper cylinder body to enter the central tube;
the boiler water inlet cavity is arranged in the upper section of the boiler body and is positioned above the inner upper cylinder;
the plurality of boiler water tubes are arranged on the periphery of the central tube near the central tube, so that a semi-isothermal zone is formed in the region, in which the boiler water tubes are arranged, in the inner upper cylinder body, and an adiabatic zone I is formed in the region, in which the boiler water tubes are not arranged, at the periphery of the semi-isothermal zone; the upper ends of the boiler water pipes are connected with the boiler water inlet cavity;
the plurality of sleeves are sleeved on the periphery of the boiler water pipes in a one-to-one correspondence manner, the lower ends of the boiler water pipes are communicated with the corresponding sleeves, and the upper ends of the sleeves are mutually communicated to form a steam collecting cavity for collecting the heated boiler water;
the steam drum is arranged above the furnace body, is communicated with the boiler water inlet cavity through a boiler water downcomer and is communicated with the steam collecting cavity through a steam rising pipe, and the steam drum, the boiler water downcomer, the boiler water inlet cavity, the boiler water column pipe, the sleeve, the steam collecting cavity and the steam rising pipe form a controllable saturated steam generating system together; and
an inner lower cylinder body which is arranged in the lower section of the furnace body and is positioned below the boiler water inlet cavity and is provided with an inner cavity for filling a shift reaction catalyst; the side wall of the furnace body is provided with an opening for mixing the mixed gas with the gas output from the lower end of the central tube, the inner lower cylinder body is provided with a second air inlet for the mixed gas to enter and an air outlet for the reacted gas to be output, and the air outlet is communicated with the conversion gas outlet.
Preferably, the lower end of the central tube extends downwards to penetrate through the inner lower cylinder, the second air inlets are arranged on the peripheral wall of the central tube in the inner lower cylinder at intervals, the air outlets are arranged on the peripheral wall of the inner lower cylinder at intervals, and an air outlet gap communicated with the conversion air outlet is arranged between the outer peripheral wall of the inner lower cylinder and the inner peripheral wall of the furnace body.
Preferably, a baffle plate positioned at the top of the inner lower cylinder body and used for preventing upward conveying of gas output by the inner lower cylinder body is arranged in the furnace body, and a mixed gas conveying pipe penetrating through the furnace body and connected with the central pipe is arranged on the side wall of the furnace body and positioned between the baffle plate and the baffle plate.
The inner lower cylinder body of the invention can also adopt another structure: the partial inner peripheral wall of the furnace body forms the peripheral wall of an inner cylinder body and a lower cylinder body, and the inner cylinder body is penetrated up and down so that the upper end of the inner cylinder body forms the second air inlet and the lower end of the inner cylinder body forms the air outlet; the inner bottom wall of the furnace body forms a bowl-shaped flow guiding structure, and the converted gas outlet is arranged at the central part of the flow guiding structure, so that the gas output from the bottom of the inner lower cylinder body is guided by the flow guiding structure and then is output from the converted gas outlet. Compared with the above structure, the structure is used for adapting to different gasification technologies and conversion process flows, has large catalyst loading and can reduce equipment size.
Preferably, a guide piece which is positioned below the partition plate and at the top of the inner lower cylinder and is in an inverted bowl-shaped structure is arranged in the furnace body, the lower end of the central tube is connected with the guide piece, a mixed gas conveying pipe which penetrates through the furnace body and is connected with the central tube is arranged on the side wall of the furnace body, and the mixed gas conveying pipe is positioned between the partition plate and the guide piece.
As another mode of adding the mixed gas, the central tube passes through the partition plate to extend outwards to the outside of the furnace body, bends back into the furnace body and conveys the gas downwards, the central tube positioned outside the furnace body forms an outer mixing tube, the bottom of the outer mixing tube is provided with a mixed gas inlet, and the top of the outer mixing tube is provided with a water jet.
Preferably, the number of the boiler water down pipes is at least two, the boiler water down pipes are symmetrically arranged on two sides of the boiler water inlet cavity, and at least one boiler water down pipe is provided with a regulating valve capable of controlling the fluid flow. The opening of the regulating valve is regulated to control the natural circulation ratio of water and gas in the system, so that the purposes of regulating the temperature of the converted gas and the saturated steam yield in the semi-isothermal reaction zone are achieved. The number, arrangement range and density of the boiler water tubes in the semi-isothermal zone can be adjusted according to the water-gas ratio of the crude synthesis gas, the load range and the temperature requirement of the shift gas outlet, so that the heat of partial shift gas reaction is transferred away by the boiler water in the semi-isothermal zone, and the shift reaction in the zone is between adiabatic and isothermal reactions.
Preferably, the inner top wall of the furnace body forms an inverted bowl-shaped flow guiding surface, the coarse synthesis gas inlet is positioned at the central part of the flow guiding surface, and the flow guiding surface forms a flow guiding structure for guiding the coarse synthesis gas to an air inlet annular gap around the coarse synthesis gas. This structure is favorable to improving the circulation effect when gas is input.
Preferably, the furnace body is provided with a catalyst loading and unloading hole I corresponding to the bottom of the inner upper cylinder body and a catalyst loading and unloading hole II corresponding to the bottom of the inner lower cylinder body so as to facilitate the replacement of the catalyst; and an inspection manhole is also formed on the side wall of the furnace body corresponding to the mixing region, so that the inspection is facilitated.
Preferably, the top and the bottom of the inner upper cylinder and the inner lower cylinder are filled with porcelain balls for protecting and supporting the shift catalyst; the top of the inner upper cylinder and the top of the inner lower cylinder are also provided with a pressing grid covered on the top of the porcelain ball, and the porcelain ball and the catalyst can be replaced by removing the pressing grid.
The invention can quickly and effectively adjust the temperature of the conversion gas by arranging the controllable semi-isothermal saturated steam generating system with the regulating valve and the bypass air inlet, has no influence on the pressure of the generated gas, and solves the problems of easy overtemperature and difficult temperature control of the conversion reaction of the feed gas with high carbon monoxide content.
Compared with the prior art, the invention has the advantages that:
according to the invention, through a sectional reaction technology, gas entering a bypass does not need to be independently heated to the activation temperature, the activation temperature can be achieved through a method of mixing the gas with the change gas at the upper section outlet of the change furnace, and the complexity of a process and equipment investment are reduced; the semi-isothermal zone is formed in the upper section by combining a controllable steam generation system, and the temperature of a conversion gas outlet can be effectively regulated by controlling the bypass air inflow and the boiler water flow according to the load of the crude synthetic gas or the water-gas ratio and the initial and final stage working conditions of the conversion catalyst, so that the stability of a downstream heat exchange system is ensured;
according to the invention, the temperature of the outlet of the conversion gas can be flexibly controlled by controlling the working condition of the semi-isothermal zone, so that the high-pressure saturated steam is overheated, an external overheat furnace or other devices are not required to be arranged for heat combination, the flow of the existing conversion process is shortened, and the investment and the operation difficulty are reduced;
the invention has wide application range, and can be applied to raw materials with carbon monoxide dry basis volume content of 30-90% and water/absolute dry gas volume ratio of 0.1-1.6; the boiler water tube array in the conversion furnace does not need to be fully distributed in the whole reactor, the number of tube arrays and sleeves is greatly reduced, the number of the tube orifices of the boiler water inlet cavity and the steam collecting cavity is reduced, and the manufacturing process difficulty is reduced.
Drawings
FIG. 1 is a schematic structural diagram of embodiment 1 of the present invention;
FIG. 2 is a cross-sectional view taken along the line A-A in FIG. 1;
FIG. 3 is a schematic structural diagram of embodiment 2 of the present invention;
FIG. 4 is a schematic structural diagram of embodiment 3 of the present invention;
fig. 5 is a schematic structural diagram of embodiment 4 of the present invention.
Detailed Description
The invention is described in further detail below with reference to the embodiments of the drawings.
Example 1:
as shown in fig. 1 and 2, the sleeve-type controllable semi-isothermal shift converter comprises a vertically extending cylindrical furnace body 27, wherein a coarse synthesis gas inlet 4 is formed in the top of the furnace body 27, a shift gas outlet 21 is formed in the bottom of the furnace body, a partition board 1c capable of dividing the inner cavity of the furnace body into an upper section 1a and a lower section 1b which are relatively independent is arranged in the furnace body 27, and the sleeve-type controllable semi-isothermal shift converter further comprises an inner upper cylinder 2a, a central pipe 22, a boiler water inlet cavity 5, a steam collecting cavity 6, a boiler water column pipe 11, a sleeve 23, a steam drum 2 and an inner lower cylinder 2b.
The inner upper cylinder 2a is provided in the upper section 1a of the furnace body 27, and has an inner cavity for filling the adiabatic shift reaction catalyst 8, an air inlet annular space 10 is formed between the outer peripheral wall of the inner upper cylinder 2a and the inner peripheral wall of the furnace body 27, and a plurality of first air inlets 20 are provided on the outer peripheral wall of the inner upper cylinder 2a at intervals.
The central tube 22 is disposed at the central portion of the inner upper cylinder 2a, the upper end is closed, the lower end is provided with a lower port communicated with the lower portion of the partition plate 1c, and a plurality of air vents 211 for allowing the air in the inner upper cylinder 2a to enter the central tube 22 are formed in the peripheral wall of the central tube 22.
The boiler water inlet chamber 5 is provided in the upper section 1a of the furnace 27 and above the inner upper cylinder 2 a.
The boiler water tubes 11 are a plurality of, each boiler water tube 11 is arranged around the periphery of the central tube 22 near the central tube 22, so that a semi-isothermal zone 9 is formed in the region of the inner upper cylinder 2a where the boiler water tube 11 is arranged, and a heat insulation zone I7 is formed in the region which is positioned at the periphery of the semi-isothermal zone 9 and is not provided with the boiler water tube 11; the upper end of each boiler water tube 11 is connected with the boiler water inlet cavity 5.
The plurality of sleeves 23 are sleeved on the periphery of the boiler water column pipes 11 in a one-to-one correspondence manner, the lower ends of the boiler water column pipes 11 are communicated with the corresponding sleeves 23, and the upper ends of the sleeves 23 are mutually communicated to form a steam collecting cavity 6 for collecting steam generated by heating boiler water.
The steam drum 2 is arranged above the furnace body 27, the top of the steam drum 2 is provided with a steam outlet 1, the steam drum 2 is communicated with the boiler water inlet cavity 5 through the boiler water down pipe 3 and is communicated with the steam collecting cavity 6 through the steam rising pipe 16, and the steam drum 2, the boiler water down pipe 3, the boiler water inlet cavity 5, the boiler water tube 11, the sleeve 23, the steam collecting cavity 6 and the steam rising pipe 16 jointly form a controllable saturated steam generating system.
The inner lower cylinder 2b is disposed in the lower section 1b of the furnace 27 and below the boiler water inlet cavity 5, and has an inner cavity for filling the shift reaction catalyst, the inner lower cylinder 2b forms an adiabatic area II 15, an opening for mixing the mixed gas with the gas output from the lower end of the central tube 22 is formed on the sidewall of the furnace 27, and the inner lower cylinder 2b has a second gas inlet 21b for the mixed gas to enter and a gas outlet 22b for the reacted gas to output, and the gas outlet 22b is communicated with the shift gas outlet 21.
The lower end of the central tube 22 extends downwards to penetrate into the inner lower cylinder 2b, a plurality of second air inlets 21a are formed in the peripheral wall of the central tube 22 in the inner lower cylinder 2b at intervals, a plurality of air outlets 22b are formed in the peripheral wall of the inner lower cylinder 2b at intervals, and an air outlet gap 23b communicated with the conversion air outlet 21 is formed between the outer peripheral wall of the inner lower cylinder 2b and the inner peripheral wall of the furnace body 27.
A baffle 24b is arranged in the furnace body 27 and positioned at the top of the inner lower cylinder 2b to prevent the gas output by the inner lower cylinder 2b from being conveyed upwards, a mixed gas conveying pipe 25 which penetrates through the furnace body 27 and is connected with the central pipe 22 is arranged on the side wall of the furnace body 27, and the mixed gas conveying pipe 25 is positioned between the baffle 1c and the baffle 24 b.
The two boiler water down pipes 3 are symmetrically arranged at two sides of the boiler water inlet cavity 5, and one boiler water down pipe 3 is provided with a regulating valve 17 capable of controlling the fluid flow. The natural circulation ratio of the water and the gas in the system is controlled by adjusting the opening of the adjusting valve 17, so that the purposes of adjusting the temperature of the converted gas and the saturated steam yield in the semi-isothermal reaction zone are achieved. The number, arrangement range and density of the boiler water tubes in the semi-isothermal zone can be adjusted according to the water-gas ratio of the crude synthesis gas, the load range and the temperature requirement of the shift gas outlet, so that the heat of partial shift gas reaction is transferred away by the boiler water in the semi-isothermal zone, and the shift reaction in the zone is between adiabatic and isothermal reactions.
The inner top wall of the furnace body 27 forms an inverted bowl-shaped flow guiding surface 191, the raw synthesis gas inlet 4 is positioned at the central part of the flow guiding surface 191, the flow guiding surface 191 forms a flow guiding structure for guiding the raw synthesis gas to the air inlet annular gap 10 around the raw synthesis gas, and the structure is beneficial to improving the circulation effect during gas input.
The furnace body 27 is provided with a catalyst loading and unloading hole I26 corresponding to the bottom of the inner upper cylinder 2a and a catalyst loading and unloading hole II28 corresponding to the bottom of the inner lower cylinder 2b so as to facilitate the replacement of the catalyst; an inspection manhole 13 is also formed on the side wall of the furnace body 27 corresponding to the space between the baffle plate 1c and the baffle plate 24b, so as to facilitate inspection.
The top and bottom of the inner upper cylinder 2a and the inner lower cylinder 2b are filled with porcelain balls 12 for protecting and supporting the shift catalyst; the tops of the inner upper cylinder 2a and the inner lower cylinder 2b are also provided with a pressing grid 19 which covers the tops of the porcelain balls 12, and the porcelain balls and the catalyst can be replaced by removing the pressing grid 19.
The use process of this embodiment is as follows:
the raw material gas of the crude synthesis gas inlet 4 enters an air inlet annular gap 10 through an upper end socket of the shift converter, passes through an adiabatic shift reaction catalyst 8 from the axial direction through a first air inlet hole 22, firstly enters an adiabatic region I6 for adiabatic shift reaction to 420 ℃, and then enters a semi-isothermal region 9; the conversion gas carries out semi-isothermal conversion reaction in the semi-isothermal zone 9, the temperature is kept unchanged, redundant heat is absorbed by boiler water in the sleeve 23 of the semi-isothermal zone to generate saturated steam, and the converted gas after the reaction is collected through the central tube 22 and enters the lower section of the conversion furnace; the temperature of the crude synthesis gas from the bypass air inlet is 210 ℃, the crude synthesis gas is fully mixed with the conversion gas at the upper section outlet of the conversion furnace through the mixed gas conveying pipe 25, then enters the heat insulation zone II14 at the lower section of the conversion furnace for carrying out heat insulation reaction again, the temperature of the gas after the reaction is 400 ℃, and the gas is led out from the conversion gas outlet 21;
in the process, the operation flow of the controllable saturated steam generation system is as follows: the low-temperature boiler water from the boiler water downcomer 3 firstly enters the boiler water inlet cavity 5 to be collected, then enters the boiler water tube 11 and the sleeve 23 in the semi-isothermal zone, and becomes a water-vapor mixture after absorbing the heat of the reaction in the semi-isothermal zone 9, wherein saturated steam rises to the steam collecting cavity 6 along the sleeve 23 for preliminary liquid separation, then continuously enters the steam drum 2 along the steam rising pipe 16, and after condensate water is separated again, saturated steam is produced from the steam outlet 1 and is sent out of the system.
The embodiment can quickly and effectively adjust the temperature of the conversion gas by arranging the controllable semi-isothermal saturated steam generating system with the regulating valve 17 and the bypass air inlet, has no influence on the pressure of the generated gas, and solves the problems that the conversion reaction of the raw gas with high carbon monoxide content is easy to overtemperature and difficult to control the temperature. The existing common semi-isothermal shift furnace outlet shift gas is required to be stabilized above a certain temperature to maintain a certain degree of superheat, and under the working condition that the load of the crude synthesis gas is changed or the activity of the catalyst is reduced at the end, a means for effectively regulating the outlet temperature is lacked, so that the controllability and the regulation are poor. In the sectional controllable semi-isothermal shift converter of the embodiment, the bypass can adjust the water-gas ratio and the CO content of mixed shift gas entering the heat insulation section; meanwhile, the heat insulation section adopts thermodynamic equilibrium control, so that the temperature requirement of the outlet change gas can be met. Therefore, the temperature range of the semi-isothermal section outlet of the sectionalized controllable semi-isothermal shift converter has no requirement, and the temperature of the heat-insulating section outlet shift gas can be ensured to be above a certain temperature (usually 400 ℃), so that the control is flexible, the operation is simple and convenient, and the stability of a downstream heat exchange network is ensured.
Example 2:
this embodiment differs from embodiment 1 in that: as shown in fig. 3, the partial inner peripheral wall of the furnace body 27 forms the peripheral wall of the inner lower cylinder 2b, and the inner lower cylinder 2b penetrates up and down so that the upper end thereof forms the second air inlet 21b and the lower end thereof forms the air outlet 22b. The inner bottom wall of the furnace body 27 forms a bowl-shaped flow guiding structure 192, and the converted gas outlet 21 is arranged at the central part of the flow guiding structure 192, so that the gas output from the bottom of the inner lower cylinder 2b is guided by the flow guiding structure 192 and then is output from the converted gas outlet 21. This structure is to accommodate different gasification technologies and shift process flows, and has a large catalyst loading and a reduced equipment size compared with the structure of example 1.
The furnace body 27 is provided with a guide piece 193 which is positioned below the partition plate 1c and at the top of the inner lower cylinder body 2b and is in an inverted bowl-shaped structure, the lower end of the central tube 22 is connected with the guide piece 193, the side wall of the furnace body 27 is provided with a mixed gas conveying pipe 25 which penetrates through the furnace body 27 and is connected with the central tube 22, and the mixed gas conveying pipe 25 is positioned between the partition plate 1c and the guide piece 193.
Example 3:
this embodiment differs from embodiment 1 in that: as shown in fig. 4, the central tube 22 passes through the partition plate 1c to extend outwards to the outside of the furnace body 27, and then bends back into the furnace body 27 to convey the gas downwards, the central tube 22 positioned outside the furnace body 27 forms an outer mixing tube 29, the bottom of the outer mixing tube 29 is provided with a mixed gas inlet 24, and the top of the outer mixing tube is provided with a water spray opening 25.
In the structure of this embodiment, water can be supplied through the water jet 25 when the gas after the reaction in the upper stage 1a is mixed with the external mixing chamber.
Example 4:
this embodiment differs from embodiment 2 in that: as shown in fig. 5, the central tube 22 passes through the partition plate 1c to extend outwards to the outside of the furnace body 27, and then bends back into the furnace body 27 to convey the gas downwards, the central tube 22 positioned outside the furnace body 27 forms an outer mixing tube 29, the bottom of the outer mixing tube 29 is provided with a mixed gas inlet 24, and the top of the outer mixing tube is provided with a water spray opening 25.
In the structure of this embodiment, water can be supplied through the water jet 25 when the gas after the reaction in the upper stage 1a is mixed with the external mixing chamber.
In the description and claims of the present invention, terms indicating directions, such as "front", "rear", "upper", "lower", "left", "right", "side", "top", "bottom", etc., are used to describe various example structural parts and elements of the present invention, but these terms are used herein for convenience of description only and are determined based on the example orientations shown in the drawings. Because the disclosed embodiments of the invention may be arranged in a variety of orientations, the directional terminology is used for purposes of illustration and is in no way limiting, such as "upper" and "lower" are not necessarily limited to being in a direction opposite or coincident with the direction of gravity.
Claims (9)
1. The utility model provides a controllable semi isothermal shift converter of bushing type, includes vertical extension and is cylindric furnace body, and open at this furnace body top has thick synthetic gas import, bottom open has shift gas export, its characterized in that: the furnace body is internally provided with a baffle plate which can divide the inner cavity of the furnace body into an upper section and a lower section which are relatively independent, and the sleeve type controllable semi-isothermal shift furnace further comprises:
an inner upper cylinder body is arranged in the upper section of the furnace body and is provided with an inner cavity for filling a heat insulation conversion reaction catalyst, an air inlet annular gap is formed between the outer peripheral wall of the inner upper cylinder body and the inner peripheral wall of the furnace body, and a plurality of first air inlets which are arranged at intervals are formed on the outer peripheral wall of the inner upper cylinder body;
the central tube is arranged at the central part of the inner upper cylinder body, the upper end of the central tube is closed, the lower end of the central tube is provided with a lower port communicated with the lower part of the partition plate, and the peripheral wall of the central tube is provided with a plurality of air vents for allowing the gas in the inner upper cylinder body to enter the central tube;
the boiler water inlet cavity is arranged in the upper section of the boiler body and is positioned above the inner upper cylinder;
the plurality of boiler water tubes are arranged on the periphery of the central tube near the central tube, so that a semi-isothermal zone is formed in the region, in which the boiler water tubes are arranged, in the inner upper cylinder body, and an adiabatic zone I is formed in the region, in which the boiler water tubes are not arranged, at the periphery of the semi-isothermal zone; the upper ends of the boiler water pipes are connected with the boiler water inlet cavity;
the plurality of sleeves are sleeved on the periphery of the boiler water column pipes in a one-to-one correspondence manner, the lower ends of the boiler water column pipes are communicated with the corresponding sleeves, and the upper ends of the sleeves are mutually communicated to form a steam collecting cavity for collecting steam generated by heating boiler water;
the steam drum is arranged above the furnace body, is communicated with the boiler water inlet cavity through a boiler water downcomer and is communicated with the steam collecting cavity through a steam rising pipe, and the steam drum, the boiler water downcomer, the boiler water inlet cavity, the boiler water column pipe, the sleeve, the steam collecting cavity and the steam rising pipe form a controllable saturated steam generating system together; and
an inner lower cylinder body which is arranged in the lower section of the furnace body and is positioned below the boiler water inlet cavity and is provided with an inner cavity for filling a shift reaction catalyst; the side wall of the furnace body is provided with an opening for mixing the mixed gas with the gas output by the lower end of the central tube, the inner lower cylinder body is provided with a second air inlet for the mixed gas to enter and an air outlet for the reacted gas to be output, and the air outlet is communicated with the conversion gas outlet;
the boiler water inlet cavity is provided with at least two boiler water down pipes, at least one of which is provided with a regulating valve capable of controlling fluid flow.
2. The telescopic controllable semi-isothermal shift converter according to claim 1, wherein: the lower end of the central tube downwards extends into the inner lower cylinder body, the second air inlets are arranged on the peripheral wall of the central tube in the inner lower cylinder body at intervals, the air outlets are arranged on the peripheral wall of the inner lower cylinder body at intervals, and an air outlet gap communicated with the conversion air outlet is formed between the outer peripheral wall of the inner lower cylinder body and the inner peripheral wall of the furnace body.
3. The telescopic controllable semi-isothermal shift converter according to claim 2, wherein: the gas-mixing furnace is characterized in that a baffle plate positioned at the top of the inner lower cylinder body and used for preventing upward conveying of gas output by the inner lower cylinder body is arranged in the furnace body, a mixed gas conveying pipe penetrating through the furnace body and connected with a central pipe is arranged on the side wall of the furnace body, and the mixed gas conveying pipe is positioned between the baffle plate and the baffle plate.
4. The telescopic controllable semi-isothermal shift converter according to claim 1, wherein: the partial inner peripheral wall of the furnace body forms the peripheral wall of an inner cylinder body and a lower cylinder body, and the inner cylinder body is penetrated up and down so that the upper end of the inner cylinder body forms the second air inlet and the lower end of the inner cylinder body forms the air outlet; the inner bottom wall of the furnace body forms a bowl-shaped flow guiding structure, and the converted gas outlet is arranged at the central part of the flow guiding structure, so that the gas output from the bottom of the inner lower cylinder body is guided by the flow guiding structure and then is output from the converted gas outlet.
5. The telescopic controllable semi-isothermal shift converter according to claim 4, wherein: the furnace body is internally provided with a flow guide piece which is positioned below the partition plate and at the top of the inner lower cylinder body and is in an inverted bowl-shaped structure, the lower end of the central tube is connected with the flow guide piece, the side wall of the furnace body is provided with a mixed gas conveying pipe which penetrates through the furnace body and is connected with the central tube, and the mixed gas conveying pipe is positioned between the partition plate and the flow guide piece.
6. The telescopic controllable semi-isothermal shift converter according to claim 1, wherein: the central tube passes through the partition plate and extends outwards to the outside of the furnace body, then bends back into the furnace body to convey the gas downwards, the central tube positioned outside the furnace body forms an outer mixing tube, the bottom of the outer mixing tube is provided with a mixed gas inlet, and the top of the outer mixing tube is provided with a water jet.
7. The telescopic controllable semi-isothermal shift converter according to any of claims 1-6, wherein: the inner top wall of the furnace body forms an inverted bowl-shaped flow guiding surface, the coarse synthesis gas inlet is positioned at the central part of the flow guiding surface, and the flow guiding surface forms a flow guiding structure for guiding the coarse synthesis gas to an air inlet annular gap at the periphery of the flow guiding structure.
8. The telescopic controllable semi-isothermal shift converter according to any of claims 1-6, wherein: the furnace body is provided with a catalyst loading and unloading hole I corresponding to the bottom of the inner upper cylinder body and a catalyst loading and unloading hole II corresponding to the bottom of the inner lower cylinder body.
9. The telescopic controllable semi-isothermal shift converter according to any of claims 1-6, wherein: the top and the bottom of the inner upper cylinder and the inner lower cylinder are filled with porcelain balls, and the tops of the inner upper cylinder and the inner lower cylinder are also provided with a pressing grid covering the tops of the porcelain balls.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110763334.4A CN113460961B (en) | 2021-07-06 | 2021-07-06 | Sleeve type controllable semi-isothermal shift converter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110763334.4A CN113460961B (en) | 2021-07-06 | 2021-07-06 | Sleeve type controllable semi-isothermal shift converter |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113460961A CN113460961A (en) | 2021-10-01 |
| CN113460961B true CN113460961B (en) | 2023-05-05 |
Family
ID=77878712
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110763334.4A Active CN113460961B (en) | 2021-07-06 | 2021-07-06 | Sleeve type controllable semi-isothermal shift converter |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113460961B (en) |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2016119224A1 (en) * | 2015-01-30 | 2016-08-04 | 湖南安淳高新技术有限公司 | Isothermal and low temperature shift converter and shift conversion process thereof |
| CN110500904B (en) * | 2019-09-20 | 2024-03-05 | 南京聚拓化工科技有限公司 | Integrated ammonia synthesis heat recovery equipment and ammonia synthesis heat recovery process |
| CN110790227B (en) * | 2019-10-24 | 2023-03-24 | 中石化宁波工程有限公司 | Isothermal transformation hydrogen production method and isothermal transformation furnace matched with coal water slurry gasification device |
| CN110790223B (en) * | 2019-10-24 | 2023-03-14 | 中石化宁波工程有限公司 | Transformation hydrogen production method matched with coal water slurry gasification device and isothermal transformation furnace |
-
2021
- 2021-07-06 CN CN202110763334.4A patent/CN113460961B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN113460961A (en) | 2021-10-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101704513B (en) | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof | |
| CN110550602B (en) | Controllable semi-isothermal conversion process for high-concentration carbon monoxide for oxo synthesis | |
| CN110550601B (en) | Transformation process for high-concentration CO raw material gas | |
| CN101975395B (en) | Dual-cycle fluidized bed device for coal-based chemical chain process | |
| CN203075923U (en) | Axial-radial constant-temperature conversion reactor | |
| CN102234213A (en) | Complete methanation reaction device for synthesis gas | |
| CN105255532B (en) | The methanation process that a kind of fluid bed is combined with fixed bed | |
| CN113460961B (en) | Sleeve type controllable semi-isothermal shift converter | |
| CN104557371A (en) | Method for preparing hydrocarbon mixture by using one-step methanol conversion in adiabatic fixed bed reactor | |
| CN104152198B (en) | Methanation reaction process | |
| CN113460962B (en) | Long-period transformation process for adjusting water-gas ratio by one-step method for oxo synthesis | |
| CN112708478A (en) | Low water-gas ratio CO conversion device and method | |
| CN113401871B (en) | Tubular sectional controllable semi-isothermal converter | |
| CN109181782B (en) | Air-cooling and water-cooling isothermal transformation process matched with coal water slurry gasification | |
| CN109279573B (en) | Isothermal transformation process matched with coal water slurry gasification | |
| CN109054908B (en) | Isothermal transformation process matched with pulverized coal gasification | |
| CN107460013B (en) | Process for preparing natural gas through methanation of synthesis gas fluidized bed based on interstage dehydration | |
| CN109280568B (en) | Isothermal transformation process matched with pulverized coal gasification | |
| CN103435432B (en) | A kind of take petroleum naphtha as the method for raw materials for ethylene production propylene | |
| CN107129844B (en) | Process for preparing natural gas by methanation of synthesis gas fluidized bed | |
| CN113501492B (en) | Long-period transformation process for adjusting water-gas ratio by two-step method for oxo synthesis | |
| CN201439492U (en) | Shunting isothermal sulphur-resisting conversion device | |
| CN113501493B (en) | High-concentration carbon monoxide sectional heat transfer half-reaction conversion process for oxo synthesis | |
| CN113460959B (en) | High-concentration carbon monoxide full-conversion segmented heat transfer process with bypass control | |
| CN219259571U (en) | Temperature-controllable shift converter |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |