CN110787737A - Isothermal shift reactor - Google Patents
Isothermal shift reactor Download PDFInfo
- Publication number
- CN110787737A CN110787737A CN201911014596.XA CN201911014596A CN110787737A CN 110787737 A CN110787737 A CN 110787737A CN 201911014596 A CN201911014596 A CN 201911014596A CN 110787737 A CN110787737 A CN 110787737A
- Authority
- CN
- China
- Prior art keywords
- heat exchange
- steam
- exchange tubes
- pipe
- cooling water
- 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.)
- Pending
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- 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
- B01J8/001—Controlling catalytic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- 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
- B01J8/0242—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 flow within the bed being predominantly vertical
- B01J8/025—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 flow within the bed being predominantly vertical in a cylindrical shaped bed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- 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
- B01J8/0285—Heating or cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- 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
- B01J8/0292—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 with stationary packing material in the bed, e.g. bricks, wire rings, baffles
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
-
- 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
Abstract
The invention relates to an isothermal shift reactor, which comprises a furnace body, a catalyst frame arranged in the furnace body and a plurality of heat exchange tubes arranged in the catalyst frame, wherein a synthesis gas collecting pipeline is also arranged in the catalyst frame, and a cavity between the catalyst frame and the synthesis gas collecting pipeline forms a reaction cavity; the method is characterized in that: the heat exchange tubes are arranged on a plurality of concentric circumferential lines, the heat exchange tubes are uniformly arranged on the respective circumferential lines, and the arrangement intervals of the heat exchange tubes on the respective circumferential lines are gradually increased from outside to inside; the inlets of the heat exchange tubes are respectively connected with the corresponding cooling water distribution tubes, and the cooling water distribution tubes are communicated with a cooling water conveying pipeline; the outlets of the heat exchange tubes are respectively connected with steam-water collecting and distributing tubes which respectively correspond to the heat exchange tubes, and the steam-water collecting and distributing tubes are communicated with a steam conveying pipeline; the cooling water distribution pipes and the steam-water collecting distribution pipes are radially arranged on the cross section of the reaction cavity.
Description
Technical Field
The invention relates to chemical equipment, in particular to an isothermal shift reactor.
Background
The isothermal shift reactor used for CO shift usually includes a furnace body and a heat exchange tube disposed in the furnace body, and reaction heat is taken away by introducing a heat exchange medium into the heat exchange tube, thereby maintaining isothermal reaction in the reactor.
For example, the invention discloses an isothermal and adiabatic radial combined reactor disclosed in the Chinese patent application No. 201410334970.5, which is composed of an isothermal shift converter and an axial adiabatic shift converter which are stacked up and down, and has the advantages of complex equipment structure, high manufacturing difficulty and high investment.
For example, in the 'temperature-variable isothermal transformation reactor' disclosed in the Chinese patent application No. 201811160917.2, two groups of heat exchange tubes are arranged for adjusting the temperature of a bed layer, the heat exchange tubes are uniformly arranged, the equipment structure is complex, and the equipment manufacturing difficulty is high. Secondly, the reactor achieves the purpose of adjusting the temperature of a bed layer by stopping one group of heat exchange tubes, and a valve is arranged on the water side of each heat exchange tube, so that the pressure drop of a system and the risk of misoperation are increased.
In the invention disclosed in the Chinese patent application No. 201410662869.2, the heat exchange tube of the reactor is curved, so that the manufacturing difficulty is high and the pressure drop on the water side is high. Secondly, the heat exchange tubes of the reactor are arranged to be sparse outside and dense inside, the gas inlet direction of the water gas is from outside to inside, so that the reaction heat of high CO concentration conversion at the periphery of the reactor cannot be removed in time, the temperature distribution of a bed layer is not uniform, and the conversion reaction efficiency is lower.
The characteristics of the CO shift reaction: after the raw gas enters the isothermal shift reactor, because the initial concentration of CO in the raw gas is very high, the driving force of the shift reaction is large, the reaction rate is very high, a large amount of heat is released by the reaction, the concentration of CO is gradually reduced along with the progress of the shift reaction, and the exothermic heat of the reaction is also gradually reduced. Therefore, the heat exchange tubes in the isothermal shift reactor are reasonably arranged, and the method is of great importance for controlling the temperature of the inner bed layer of the reactor, improving the shift reaction efficiency and reducing the equipment investment.
The arrangement of heat exchange tubes in the existing isothermal transformation reactor mainly has two types, one is tube distribution with sparse outside and dense inside, and the other is uniform tube distribution. Both the two pipe distribution types can cause uneven heat removal in the reactor, reduce the conversion reaction efficiency and increase the equipment investment.
Secondly, the distribution pipe of the prior isothermal transformation reactor mainly has two types, one is a circular pipe, and the other is a small pipe plate. Both the two kinds of distribution pipes are nonstandard parts and need to be designed and manufactured independently, so that the manufacturing technical requirement is high and the manufacturing cost is high. For the connection of the distribution pipe and the heat exchange pipe, modularization is difficult to achieve, and the technical requirement on the group in the installation process is high.
Disclosure of Invention
The invention aims to solve the technical problem of providing an isothermal shift reactor which has uniform heat removal, high shift reaction efficiency and low equipment investment aiming at the current situation of the prior art.
The technical scheme adopted by the invention for solving the technical problems is as follows: an isothermal shift reactor comprises a furnace body, a catalyst frame arranged in the furnace body and a plurality of heat exchange tubes arranged in the catalyst frame, wherein a synthesis gas collecting pipeline is also arranged in the catalyst frame, and a cavity between the catalyst frame and the synthesis gas collecting pipeline forms a reaction cavity; the method is characterized in that:
the heat exchange tubes are arranged on a plurality of concentric circumferential lines, the heat exchange tubes are uniformly arranged on the respective circumferential lines, and the arrangement distance of the heat exchange tubes on the respective circumferential lines is gradually increased from outside to inside;
the inlet of each heat exchange tube is respectively connected with a corresponding cooling water distribution tube, and each cooling water distribution tube is communicated with a cooling water conveying pipeline; outlets of the heat exchange tubes are respectively connected with steam-water collecting and distributing tubes corresponding to the outlets, and the steam-water collecting and distributing tubes are communicated with a steam conveying pipeline;
and the cooling water distribution pipes and the steam-water collection distribution pipes are radially arranged on the cross section of the reaction cavity.
The cooling water distribution pipe comprises cooling water distribution short pipes and cooling water distribution long pipes which are arranged at intervals; the steam-water collecting distribution pipe comprises steam-water collecting distribution short pipes and steam-water collecting distribution long pipes which are arranged at intervals.
The outer ends of the long steam-water collecting and distributing pipes and the short steam-water collecting and distributing pipes are aligned, and the outer ends of the long cooling water distributing pipes and the short cooling water distributing pipes are aligned;
preferably, the cooling water distribution pipe and the steam-water collecting distribution pipe are arranged in an up-and-down symmetrical mode.
Each steam-water collecting and distributing pipe is connected with the steam conveying pipeline through an annular steam-water collecting pipe; and each cooling water distribution pipe is connected with the cooling water conveying pipeline through an annular cooling water connecting pipe.
The steam-water collecting pipe and the cooling water collecting pipe are concentrically arranged with the catalyst frame.
Each heat exchange tube is divided into an outer zone close to the catalyst frame, an inner zone close to the synthesis gas collecting tube and a middle zone between the two zones on the cross section of the reaction cavity according to the arrangement density;
the long vapor-water collecting and distributing pipes are communicated with the corresponding outer zone, the middle zone and the heat exchange pipes in the inner zone; the steam-water collecting distribution short pipes are communicated with the heat exchange pipes in the corresponding outer zone and the middle zone;
the cooling water distribution long pipe is communicated with the corresponding outer zone, the middle zone and each heat exchange pipe in the inner zone; the cooling water distribution short pipe is communicated with the corresponding outer zone and each heat exchange pipe in the middle zone.
The scheme arranges the heat exchange tubes in the reactor into three regions with different density degrees: outer zone, middle zone and inner zone. In the outer district, the heat exchange tube arranges densely, in the middle district, the heat exchange tube arranges moderately densely, and in the inner district, the heat exchange tube arranges sparsely. Compared with the traditional isothermal shift reactor, the number of the heat exchange tubes in the middle area and the inner area is obviously reduced, and the number of the heat exchange tubes in the reactor with the same scale is reduced by 15 to 25 percent, so that the equipment investment is obviously reduced.
The circumferential distance between adjacent heat exchange tubes in the outer zone is 60-90 mm; the circumferential space between adjacent heat exchange tubes in the middle area is 80-140 mm, and the circumferential space between adjacent heat exchange tubes in the inner area is 100-160 mm.
On the same radial line direction, adjacent interval between the heat exchange tube is 60 ~ 130mm, and outside-in grow gradually, and each interval becomes the arithmetic progression and arranges that the tolerance is 3 ~ 10 mm.
The circumferential distance and the radial distance of the heat exchange tubes can well control the temperature difference of a catalyst bed layer according to the characteristics of CO conversion reaction, and also consider the factors of catalyst loading and unloading, investment, welding manufacture and the like. When the distance between the heat exchange pipes is too large, the heat exchange area is small, the heat removal of a reactor bed layer is small, the high temperature difference of a catalyst bed layer is caused, and the reaction efficiency is influenced. When the distance between the heat exchange pipes is too small, the heat exchange area is increased, the low temperature difference of a catalyst bed layer can be ensured, the reaction efficiency is improved, the investment is increased, the loading and unloading of the catalyst are difficult, the welding seams of the heat exchange pipes are too close to each other, the manufacturing is difficult, and the welding seam quality is influenced by the mutual overlapping of the welding seam heat affected zones. In consideration of the characteristics of the CO conversion reaction, the raw gas flows through the outer zone, the middle zone and the inner zone in the reactor in sequence. 60% -80% of CO in the outer zone completes the shift reaction, a large amount of heat is released in the reaction, and dense heat exchange tubes are required to be arranged for heat removal, so that the circumferential distance and the radial distance between adjacent heat exchange tubes in the zone are small. The number of the heat exchange tubes arranged on the outer zone accounts for 50-70% of the total number of the heat exchange tubes. Along with the reaction, the CO content in the middle area and the inner area is gradually reduced, the reaction heat release is gradually reduced, the heat quantity to be removed is smaller and smaller, the circumferential distance and the radial distance between the heat exchange tubes are gradually increased, the arranged heat exchange tubes are gradually sparse, the number of the heat exchange tubes arranged in the middle area accounts for 20% -40% of the total number of the heat exchange tubes, and the number of the heat exchange tubes arranged in the inner area accounts for 8% -15% of the total number of the heat exchange tubes.
Preferably, the number of the heat exchange tubes arranged in the outer zone accounts for 50% -70% of the total number of the heat exchange tubes, the number of the heat exchange tubes arranged in the middle zone accounts for 20% -40% of the total number of the heat exchange tubes, and the number of the heat exchange tubes arranged in the inner zone accounts for 8% -15% of the total number of the heat exchange tubes.
Further, the radial distribution pipes are arranged, and gaps formed among the distribution pipes are beneficial to arrangement of the temperature detector. . The number of the temperature detectors can be flexibly configured according to the monitoring requirement of the catalyst bed layer temperature. Can be in the outer district, the middle district, the inner district has all set up the thermoscope, is used for detecting the temperature distribution condition in three district respectively, really feeds back catalyst bed temperature distribution condition, provides effectual detection means for reactor steady operation.
Compared with the prior art, the isothermal shift reactor provided by the invention has the following advantages:
1. according to the characteristics of CO conversion reaction, the isothermal conversion reactor adopts heat exchange tubes which are arranged in a mode of being dense outside and sparse inside and are consistent with the gas inlet direction of the crude gas; the high-low temperature area of the catalyst bed layer is matched through the density arrangement of the heat exchange tubes; the method is characterized in that the arrangement of heat exchange tubes in a high-temperature area is dense, the arrangement of heat exchange tubes in a low-temperature area is sparse, the requirements of welding, investment, loading and unloading of a catalyst, temperature difference of a catalyst bed layer and the like are met, the temperature difference of the catalyst bed layer on the same plane can be accurately controlled to be 3-5 ℃, and the axial temperature difference is controlled to be 5-15 ℃.
2. The isothermal shift reactor provided by the invention can flexibly adjust the size of the reactor according to the scale of the device, and the size of the reactor can be flexibly adjusted to adapt to treatment capacities of different scales only by changing the lengths of the cooling water distribution pipe and the steam-water collection distribution pipe, and/or increasing or reducing the number of circumferences of the heat exchange pipes, and/or changing the diameter of the cylinder.
3. The invention is particularly suitable for use as a radial isothermal reactor.
Drawings
FIG. 1 is a longitudinal sectional view of a reactor section in an embodiment of the invention;
FIG. 2 is a cross-sectional view taken along line A-A of FIG. 1;
FIG. 3 is a cross-sectional view taken along line B-B of FIG. 1;
FIG. 4 is an enlarged view of a portion of FIG. 3 taken along line C;
fig. 5 to 6 are connection structures of different numbers of heat exchange tubes and cooling water distribution tubes (vapor-water collecting distribution tubes).
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1 to 6, the isothermal shift reactor includes:
the furnace body 1 is of a conventional structure and comprises an upper seal head 11, a lower seal head 12 and a cylinder body 13 connected between the upper seal head 11 and the lower seal head 12. The upper end enclosure 11 is provided with a manhole 14, the manhole 14 is covered by a manhole cover, and the feed gas inlet 35 is arranged on the manhole cover.
And the catalyst frame 21 is used for filling a catalyst and is arranged in the cylinder body 13, and a reaction cavity is formed by a cavity between the catalyst frame 21 and the synthesis gas collecting pipeline 3. The mounting structure of the catalyst frame 21 may be any one of those in the prior art as required. In this embodiment, the upper and lower ends of the catalyst frame 21 are not closed, the upper and lower ends of the catalyst bed layer in the catalyst frame 21 are filled with refractory balls, and the catalyst frame is fixed by the cylinder 13.
A gap between the catalyst frame 21 and the side wall of the furnace body forms a feed gas channel 2 a; the synthesis gas collecting pipeline 3 is sleeved in the catalyst frame 21. A reaction chamber 2b is formed between the catalyst frame 21 and the synthesis gas collecting pipe 3.
The side walls of the catalyst frame 21 are provided with through holes (not shown in the figure), and the through holes not only serve as flow channels for raw material gas and conversion gas, but also serve as gas distributors, so that the raw material gas uniformly enters the reaction chamber.
In this embodiment, the cross-sectional structures of the cylinder, the catalyst frame, and the syngas collection tube are the same, and are concentrically arranged concentric circular structures.
The synthesis gas collecting pipeline 3 is used for collecting the conversion gas and sending the conversion gas out of the furnace body 1 through a synthesis gas conveying pipeline 33, is arranged in the catalyst frame, is coaxial with the catalyst frame, and is formed by sequentially and detachably connecting a plurality of sections of cylinder bodies 31, the length of each cylinder body 31 is 800-1200 mm, and the adjacent cylinder bodies 31 are connected through flanges 34 in the embodiment; the side wall of each cylinder 31 is provided with a plurality of air inlets (not shown in the figure) for the conversion gas to enter the synthesis gas collecting pipeline 3 from the catalyst bed layer; a plurality of footsteps 32 are sequentially arranged on the inner side wall of the cylinder 31 at intervals along the axial direction. The end cover is detachably connected to the upper end port of the synthesis gas collecting pipeline 3, and is communicated with the inner cavity of the upper end enclosure and the manhole 14 after being disassembled, so that maintainers can enter the synthesis gas collecting pipeline 3; the lower port of the synthesis gas collecting tube 3 is connected with a synthesis gas conveying pipe 33. The synthesis gas collecting pipeline 3 adopts a detachable structure, is convenient to disassemble and assemble, is favorable for the inspection and maintenance of internal parts of the reactor, and is favorable for the loading and unloading of the catalyst and the leakage detection, maintenance and replacement of subsequent heat exchange pipes.
And the steam collecting pipe is used for collecting steam-water mixture, is arranged at the upper part of the catalyst frame and is divided into a steam-water collecting pipe 57 and a steam-water collecting distribution pipe 55. The steam-water collecting pipe 57 is an annular pipe and is arranged concentrically with the cylinder, and the outlet of the annular pipe is communicated with the steam conveying pipe 58. The inlet of the annular pipeline is arranged below and is provided with a plurality of openings communicated with the collecting connecting pipes 56, and the number of the openings is the same as that of the collecting connecting pipes 56. The collecting connecting pipe 56 is used for communicating the steam-water collecting pipe 57 and the steam-water collecting distribution pipe 55.
The steam-water collecting and distributing pipes 55 are provided with a plurality of steam-water collecting and distributing pipes which are uniformly arranged in a radial direction of the cylinder body, and the steam-water collecting and distributing pipes are divided into two groups according to the length, namely a steam-water collecting and distributing short pipe 55a and a steam-water collecting and distributing long pipe 55 b. The short steam-water collecting and distributing pipes 55a and the long steam-water collecting and distributing pipes 55b are arranged in a staggered manner in sequence. The steam-water collecting and distributing pipe has pipe caps in two ends, the steam-water collecting and distributing pipe has outlet communicated with the collecting connecting pipes 56 in the upper part, and the collecting connecting pipes 56 are in the same number as the steam-water collecting and distributing pipes. The inlets of the steam-water collecting and distributing pipes are provided with a plurality of inlets which are respectively connected with the outlets of the heat exchange pipes corresponding to the inlets.
The cooling water distribution pipe is used for uniformly distributing boiler water in each heat exchange pipe, is arranged at the lower part of the catalyst frame, has the same structural form as the steam collecting distribution pipe, and comprises a cooling water connecting pipe 52 and a cooling water distribution pipe 54. The outlet of the cooling water conveying pipeline 51 is connected with the inlet of a cooling water connecting pipe 52, the outlet of the cooling water connecting pipe 52 is communicated with the inlet of a distribution connecting pipe 53, the outlet of the distribution connecting pipe 53 is communicated with the inlet of a cooling water distribution pipe 54, and the outlet of the cooling water distribution pipe 54 is communicated with the inlets of the heat exchange pipes.
The heat exchange tubes are provided with a plurality of heat exchange tubes, one end of each heat exchange tube is connected to the cooling water distribution tube 54, the other end of each heat exchange tube is connected to the steam-water collecting distribution tube 55, and the heat exchange tubes are vertically arranged in the catalyst bed layer in a penetrating mode and parallel to the axis of the furnace body 1. The heat exchange tubes are arranged on a plurality of concentric circumferential lines in the reaction cavity, the heat exchange tubes on the same circumferential line are uniformly distributed at intervals in the circumferential direction, and the heat exchange tubes are radially arranged along the radial direction of the catalyst frame. According to different density degrees arranged along the circumferential direction of the heat exchange tube, the heat exchange tube is divided into three areas, namely an outer area, a middle area and an inner area from outside to inside along the radial direction. For ease of distinction, and viewing, the heat exchange tubes of the outer zones in fig. 3-4 are represented by circles with cross-hatching ("×") and are designated outer zone heat exchange tubes 41; the middle heat exchange tube is represented by a solid circle and is named as a middle heat exchange tube 42; the inner heat exchange tubes are indicated by hollow circles and are designated as inner zone heat exchange tubes 43.
In this embodiment, the arrangement principle of each heat exchange tube is as follows: in the circumferential direction, the circumferential distance y of the outer-zone heat exchange tubes 41 is controlled to be 60-90 mm; the annular distance y between the heat exchange tubes 42 in the middle area is controlled to be 80-140 mm, and the annular distance y between the heat exchange tubes 43 in the inner area is controlled to be 100-160 mm. On the same radial line direction, the interval x of heat exchange tube radial direction is 60 ~ 130mm, and outside-in grow gradually, and the interval becomes the arithmetic progression and arranges, and adjacent radial interval differs 3 ~ 10mm, and this embodiment interval differs 3 mm.
The same circumferential section of each cooling water distribution pipe and each steam-water collecting distribution pipe and the connection of the heat exchange pipes have various forms, namely, the same section of each distribution pipe can be connected with a plurality of heat exchange pipes, and the number of the connection of the heat exchange pipes is related to the outer perimeter of the section of the distribution pipe and the size of the heat exchange pipes. In this embodiment, taking the dimensions of each cooling water distribution pipe and each steam-water collecting distribution pipe as DN200 and the heat exchange pipe phi 25 as an example, 2 typical connection forms are adopted in combination with the density form of the heat exchange pipes of the inner zone, the middle zone and the outer zone and the corresponding relationship between the cooling water distribution pipe and each steam-water collecting distribution pipe. As shown in fig. 5 and 6, the heat exchange tubes of the outer zone are dense, and the same circumferential section of each cooling water distribution tube and each steam-water collecting distribution tube is connected with six heat exchange tubes (fig. 6). The middle area and the inner area, each cooling water distribution pipe and each steam-water collecting distribution pipe have the same circumferential section and are connected with 3 heat exchange pipes (figure 5). The connecting mode is simplified, the standardization is easy, the batch industrialized production is prefabricated, the production cost is low, and the quality is high.
The raw gas enters the cavity of the upper end enclosure of the reactor through the raw gas inlet 35, descends along the raw gas channel 2a, uniformly enters the catalyst bed layer of the reaction cavity through each through hole on the catalyst frame, sequentially passes through the outer zone, the middle zone and the inner zone, and carries out CO conversion reaction in each zone. CO content of outer zone > CO content of middle zone > CO content of inner zone, i.e. heat of reaction of outer zone > heat of reaction of middle zone > heat of reaction of inner zone. 60% -80% of CO conversion reaction is completed in the outer zone, a large amount of reaction heat is generated and accumulated in the conversion reaction, dense heat exchange tubes are required to be arranged for heat removal, the CO content is gradually reduced in the middle zone and the inner zone along with the reaction, the reaction heat release is gradually reduced, the heat required to be removed is smaller and smaller, and the arranged heat exchange tubes are thinner. In this embodiment, the number of the heat exchange tubes in the outer zone accounts for about 60% of the total number of the heat exchange tubes, the number of the heat exchange tubes in the middle zone accounts for about 30% of the total number of the heat exchange tubes, and the number of the heat exchange tubes in the inner zone accounts for about 10% of the total number of the heat exchange tubes. The density arrangement of the heat exchange tubes is beneficial to uniform heat removal, and through the reasonable arrangement of the heat exchange tubes, the temperature difference of the catalyst bed layer on the same plane is controlled to be 3-5 ℃, and the axial temperature difference is controlled to be 5-15 ℃.
In order to monitor the distribution condition of the bed temperature, the reactor is provided with a plurality of temperature detectors 61, the sleeve pipes of the temperature detectors are parallel to the axis of the furnace body 1 and vertically penetrate through the catalyst bed, and a plurality of temperature measuring points are arranged in each temperature detector and used for monitoring the temperature distribution of different catalyst bed heights. The temperature detector is one of the prior art. Because the steam-water collecting and distributing pipes are radially arranged along the radial direction of the cylinder, the clearance between the steam-water collecting and distributing short pipe 55a and the steam-water collecting and distributing long pipe 55b facilitates the crossing and placement of the temperature detectors 61, and the clearance is uniformly distributed on the radial section of the cylinder, thereby being beneficial to the uniform distribution of the temperature detectors on the radial section of the cylinder. The number of the thermometers can be flexibly configured according to the monitoring requirement of the catalyst bed temperature, and 18 sets of thermometers are arranged in the embodiment and are distributed in the outer zone, the middle zone and the inner zone, and are respectively used for detecting the temperature distribution conditions of the three zones.
Each heat exchange tube is arranged in a radial shape, and the catalyst is convenient to unload. During maintenance, tools can be inserted into gaps between adjacent radioactive rays for accumulated catalyst blocks so as to conveniently break the catalyst blocks; meanwhile, the filling of the catalyst is facilitated, when the catalyst is filled, the catalyst is simply poured into the catalyst frame from the upper part, catalyst particles can fall along gaps among the heat exchange tubes, and the gaps are unobstructed from top to bottom, so that the catalyst cannot be blocked in the falling process, and the inner cavity of the whole catalyst frame can be uniformly distributed.
The steam delivery pipe 58 is provided with an expansion joint 58a for absorbing thermal stress.
The working principle of the isothermal shift reactor is described as follows:
the raw gas enters the cavity of the upper end enclosure of the reactor through the raw gas inlet 35, goes down along the raw gas channel, uniformly enters the catalyst bed layer of the reaction cavity through each through hole on the catalyst frame, and sequentially passes through the outer zone, the middle zone and the inner zone to carry out CO conversion reaction to form conversion gas. Boiler water in a steam drum (not shown in the figure) enters each heat exchange tube through a cooling water conveying pipe, a cooling water connecting pipe, a distribution connecting pipe and a cooling water distribution pipe in a natural circulation mode, reaction heat of a catalyst bed layer in a reaction cavity is taken away, a generated steam-water mixture returns to the steam drum through a steam-water collecting pipe, a collection connecting pipe, a steam-water collecting pipe and a steam conveying pipe to carry out steam-liquid separation, and saturated steam is obtained as a byproduct. The shifted gas is delivered to the downstream system through the syngas header 3 via the syngas delivery conduit 33.
The cooling water distribution pipe and the steam-water collecting distribution pipe in the embodiment can adopt standard parts, and in the outer area, each heat exchange pipe is connected with the cooling water distribution pipe and the steam-water collecting distribution pipe in the same type; in the middle area and the inner area, each heat exchange tube is connected with a cooling water distribution tube and a steam-water collecting distribution tube in the same type; the cooling water distribution pipe and the steam-water collecting distribution pipe are arranged in an up-and-down symmetrical manner; the integral structure of the equipment and the structure of each heat exchange pipe are simple, and the connecting structure of the radial distribution pipes and the heat exchange pipes can realize the modular design and manufacture of the equipment, effectively shorten the manufacturing period of the equipment and reduce the manufacturing cost of the equipment.
Each heat exchange tube is respectively connected to each radial distribution tube. The distribution pipe is provided with a plurality of circumferential sections in the polar axis direction; the polar shaft arrangement form of the distribution pipe is beneficial to realizing the arrangement structure of the heat exchange pipe with dense outside and sparse inside, is convenient for realizing standardized modular manufacturing, is beneficial to factory batch manufacturing, shortens the manufacturing period of equipment, reduces the manufacturing cost of the equipment and improves the manufacturing quality of the equipment.
Claims (10)
1. An isothermal shift reactor comprises a furnace body, a catalyst frame arranged in the furnace body and a plurality of heat exchange tubes arranged in the catalyst frame, wherein a synthesis gas collecting pipeline is also arranged in the catalyst frame, and a cavity between the catalyst frame and the synthesis gas collecting pipeline forms a reaction cavity; the method is characterized in that:
the heat exchange tubes are arranged on a plurality of concentric circumferential lines, the heat exchange tubes are uniformly arranged on the respective circumferential lines, and the arrangement distance of the heat exchange tubes on the respective circumferential lines is gradually increased from outside to inside;
the inlet of each heat exchange tube is respectively connected with a corresponding cooling water distribution tube, and each cooling water distribution tube is communicated with a cooling water conveying pipeline; outlets of the heat exchange tubes are respectively connected with steam-water collecting and distributing tubes corresponding to the outlets, and the steam-water collecting and distributing tubes are communicated with a steam conveying pipeline;
and the cooling water distribution pipes and the steam-water collection distribution pipes are radially arranged on the cross section of the reaction cavity.
2. Isothermal shift reactor according to claim 1, characterized in that said cooling water distribution tubes comprise short cooling water distribution tubes and long cooling water distribution tubes arranged at intervals; the steam-water collecting distribution pipe comprises steam-water collecting distribution short pipes and steam-water collecting distribution long pipes which are arranged at intervals.
3. The isothermal shift reactor according to claim 2, wherein the long vapor-water collecting and distributing pipe is aligned with the outer end of the short vapor-water collecting and distributing pipe, and the long cooling-water distributing pipe is aligned with the outer end of the short cooling-water distributing pipe.
4. Isothermal shift reactor according to claim 3, characterized in that said cooling water distribution pipes and said steam-water collecting distribution pipes are arranged in an up-down symmetrical manner.
5. Isothermal shift reactor according to claim 1, characterized in that each said steam-water collecting distribution pipe is connected to said steam delivery pipe by an annular steam-water collecting pipe; and each cooling water distribution pipe is connected with the cooling water conveying pipeline through an annular cooling water connecting pipe.
6. Isothermal shift reactor according to claim 5, characterized in that said steam-water collection pipe and said cooling-water collection pipe are arranged concentrically with said catalyst frame.
7. Isothermal shift reactor according to any of claims 1 to 6, characterized in that each of said heat exchange tubes is divided in arrangement density over the cross section of said reaction chamber into an outer zone adjacent to said catalyst frame, an inner zone adjacent to said synthesis gas collection tube and a middle zone located therebetween;
the long vapor-water collecting and distributing pipes are communicated with the corresponding outer zone, the middle zone and the heat exchange pipes in the inner zone; the steam-water collecting distribution short pipes are communicated with the heat exchange pipes in the corresponding outer zone and the middle zone;
the cooling water distribution long pipe is communicated with the corresponding outer zone, the middle zone and each heat exchange pipe in the inner zone; the cooling water distribution short pipe is communicated with the corresponding outer zone and each heat exchange pipe in the middle zone.
8. The isothermal shift reactor of claim 7, wherein the circumferential spacing between adjacent heat exchange tubes in the outer zone is 60-90 mm; the circumferential space between adjacent heat exchange tubes in the middle area is 80-140 mm, and the circumferential space between adjacent heat exchange tubes in the inner area is 100-160 mm.
9. The isothermal shift reactor according to claim 8, wherein in the same radial line direction, the spacing between adjacent heat exchange tubes gradually increases from outside to inside, and the spacings are arranged in an equal-difference array with a tolerance of 3-10 mm.
10. The isothermal shift reactor according to claim 9, wherein the number of the heat exchange tubes disposed at the outer zone accounts for 50-70% of the total number of the heat exchange tubes, the number of the heat exchange tubes disposed at the middle zone accounts for 20-40% of the total number of the heat exchange tubes, and the number of the heat exchange tubes disposed at the inner zone accounts for 8-15% of the total number of the heat exchange tubes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911014596.XA CN110787737A (en) | 2019-10-24 | 2019-10-24 | Isothermal shift reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911014596.XA CN110787737A (en) | 2019-10-24 | 2019-10-24 | Isothermal shift reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110787737A true CN110787737A (en) | 2020-02-14 |
Family
ID=69441108
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911014596.XA Pending CN110787737A (en) | 2019-10-24 | 2019-10-24 | Isothermal shift reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110787737A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110925722A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Isothermal transformation process and isothermal transformation furnace matched with coal chemical device |
| WO2022214069A1 (en) * | 2021-04-09 | 2022-10-13 | 中国石油化工股份有限公司 | Heat removal pipe group, method for controlling reaction temperature, and method for fabricating unsaturated nitriles |
| CN116753750A (en) * | 2023-08-21 | 2023-09-15 | 南京华兴压力容器制造有限公司 | Devolatilization preheating device and preheating method suitable for high-viscosity polymer |
-
2019
- 2019-10-24 CN CN201911014596.XA patent/CN110787737A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110925722A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Isothermal transformation process and isothermal transformation furnace matched with coal chemical device |
| WO2022214069A1 (en) * | 2021-04-09 | 2022-10-13 | 中国石油化工股份有限公司 | Heat removal pipe group, method for controlling reaction temperature, and method for fabricating unsaturated nitriles |
| CN116753750A (en) * | 2023-08-21 | 2023-09-15 | 南京华兴压力容器制造有限公司 | Devolatilization preheating device and preheating method suitable for high-viscosity polymer |
| CN116753750B (en) * | 2023-08-21 | 2023-11-03 | 南京华兴压力容器制造有限公司 | Devolatilization preheating device and preheating method suitable for high-viscosity polymer |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110787737A (en) | Isothermal shift reactor | |
| CN207102558U (en) | A kind of modularization temperature control reactor | |
| CN109261081B (en) | Temperature-variable isothermal shift reactor | |
| CN211436143U (en) | Isothermal shift reactor | |
| WO2013004254A1 (en) | Heat exchange reactor | |
| CN105664804A (en) | Axial-radial isothermal reactor | |
| CN102886229B (en) | CO (carbon monoxide) full-radial isothermal converting furnace | |
| CN109111342B (en) | Water-cooling methanol synthesis process | |
| CN109173936B (en) | Methanol synthesis water-cooling reactor | |
| CN108905906B (en) | Axial-radial reactor | |
| CN109052318B (en) | Isothermal shift reactor | |
| CN110925722B (en) | Isothermal transformation process and isothermal transformation furnace matched with coal chemical device | |
| CN108970548A (en) | Equal temperature shift reactions device | |
| CN109232179B (en) | Methanol synthesis process | |
| CN109225075B (en) | Temperature-variable isothermal methanol synthesis reactor | |
| CN110921618B (en) | Air-cooled transformation series isothermal transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace | |
| CN110921620B (en) | Isothermal transformation parallel adiabatic transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace | |
| CN110803681B (en) | Gas-cooled transformation series isothermal transformation hydrogen production process matched with coal water slurry gasification and isothermal transformation furnace | |
| CN110921617B (en) | Isothermal transformation parallel air-cooled transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace | |
| CN110898769B (en) | Poly-generation isothermal transformation process matched with pulverized coal gasification process and isothermal transformation furnace | |
| CN110921621B (en) | Low-steam-ratio poly-generation isothermal transformation process and isothermal transformation furnace matched with pulverized coal gasification | |
| CN109012506B (en) | Methanol synthesis water-cooling reactor | |
| CN111086972B (en) | CO isothermal conversion process and isothermal conversion furnace matched with pulverized coal gasification | |
| CN109225074B (en) | Temperature-variable isothermal shift reactor | |
| CN109173937B (en) | Temperature-variable methanol synthesis reaction system |
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 |