CN112808178B - Reaction device and method for preparing 3-hydroxypropionaldehyde by acrolein hydration - Google Patents
Reaction device and method for preparing 3-hydroxypropionaldehyde by acrolein hydration Download PDFInfo
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- CN112808178B CN112808178B CN202011613603.0A CN202011613603A CN112808178B CN 112808178 B CN112808178 B CN 112808178B CN 202011613603 A CN202011613603 A CN 202011613603A CN 112808178 B CN112808178 B CN 112808178B
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- 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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
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- 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
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/00044—Temperature measurement
- B01J2208/00053—Temperature measurement of the heat exchange medium
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- 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
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
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Abstract
The invention relates to the field of chemical industry, and discloses a reaction device and a method for preparing 3-hydroxypropionaldehyde by acrolein hydration, wherein in the device, a catalyst is filled in a tube nest, raw materials are fed from a feed inlet, flow through the catalyst in the tube nest, and are discharged from a discharge outlet, and the tube pass is followed; the heat removing medium is fed from the medium removing inlet of the annular channel and discharged from the medium removing outlet. The device of the invention is characterized in that: a feed distribution plate is arranged at the feed inlet, the tube array is an axial inner finned tube, and a catalyst is filled in the tube; the shell pass media removing material inlet and outlet are provided with annular channels, and the cylindrical wall of the shell pass in the annular channels is provided with uniformly distributed media removing through holes; the shell pass adopts a disc-annular guide plate, and the center and the edge of the tube plate are respectively provided with a non-cloth tube area. The device with the structure can realize uniform flow and uniform heat exchange of materials, and control the reaction temperature within a reasonable small range.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a reaction device and a method for preparing 3-hydroxypropionaldehyde by acrolein hydration.
Background
PTT is called as 'intelligent' polymer and is widely applied to the fields of textile, carpet and engineering plastics, and fibers prepared from PTT have more excellent performance and wider application than terylene and nylon fibers. One of the main raw materials for synthesizing the novel polyester PTT is 1,3 propylene glycol, and the preparation of the 1,3 propylene glycol by further hydrogenating 3-hydroxypropionaldehyde prepared by acrolein hydration is one of the main production processes at present.
At present, domestic researches on preparing 1, 3-propanediol by hydrating acrolein are focused on the selection of catalysts more, and researches on production devices involved in the process are less. In the prior art, the tubular fixed bed reactor is suitable for the hydration reaction of preparing 1,3 propanediol from acrolein. However, the main problems of the tubular fixed bed reactor commonly used in the industry at present are: after materials enter a reactor, the materials react under the action of catalysts in tubes under certain temperature and pressure, part of heat generated by the reaction is taken away by the reaction materials, and most of the heat needs to be taken away by heat removal media on the shell side of the reactor; for exothermic reaction, especially when the exothermic quantity is large, the local temperature of the catalyst bed is easily high, even the temperature runaway phenomenon occurs, and the service life and the reaction efficiency of the catalyst are seriously influenced.
Disclosure of Invention
In order to solve the technical problem, the invention provides a reaction device and a method for preparing 3-hydroxypropionaldehyde by acrolein hydration. The device can meet the hydration reaction characteristics of preparing 3-hydroxy-propionaldehyde from acrolein, and has the advantages of uniform material distribution and heat transfer, high reaction efficiency, high production stability and low energy consumption. The device of the invention is not only suitable for preparing 3-hydroxypropionaldehyde by acrolein hydration, but also suitable for other reactions with similar reaction conditions.
The specific technical scheme of the invention is as follows:
in a first aspect, the present invention provides a reaction apparatus for preparing 3-hydroxypropanal by hydration of acrolein, comprising:
the top surface and the bottom surface of the shell side cylinder are respectively provided with a tube plate; the tube plate is provided with tube holes; the central area and the edge area of the tube plate are respectively a central circular non-cloth tube area and an edge annular non-cloth tube area.
And the plurality of tubes are axially arranged in the shell pass cylinder body, catalysts are filled in the tubes, and two ends of each tube are respectively communicated with tube array holes of the tube plates on the top surface and the bottom surface of the shell pass cylinder body. Each row tube is internally provided with a plurality of high-rib inner fins which are axially arranged, and the inner fins are distributed on the cross section of the row tube at equal angles.
The circular guide plates and the annular guide plates are axially and alternately arranged in the shell pass cylinder to form a zigzag medium removing flow channel; the outer diameter of the circular guide plate corresponds to the inner diameter of the edge annular non-distribution pipe area, and the inner diameter of the annular guide plate corresponds to the outer diameter of the central circular non-distribution pipe area.
The media removing inlet and the media removing outlet are directly or indirectly arranged on the outer side wall of the shell pass cylinder.
And the upper end enclosure is covered on the top of the shell pass cylinder body, and a feed inlet or a discharge outlet is arranged on the upper end enclosure.
And the lower end enclosure is covered at the bottom of the shell pass cylinder body, and is provided with a discharge port or a feed port.
And the feeding distribution plate is arranged between the top surface or the bottom surface of the shell pass cylinder and the feeding hole.
The heat release of the hydration reaction for preparing the 3-hydroxypropionaldehyde by acrolein hydration is large, the requirement on the reaction temperature is strict, the allowable change interval of the reaction temperature is small, and the influence of the temperature on the proportion of side reaction and the selectivity of the 3-hydroxypropionaldehyde is large, so that the realization of uniform distribution and uniform heat transfer of reaction materials are key factors considered during the design of a reactor.
The working principle of the device is as follows: filling a catalyst into the tubes, feeding a mixed solution of raw material acrolein and water from a feed inlet of the lower end enclosure or the upper end enclosure, moving the mixed solution away from the tube pass, uniformly distributing the mixed solution to inlets of the tubes through a feed distribution plate, allowing the mixed solution to flow through the catalyst in the tubes, and discharging the mixed solution from a discharge outlet of the lower end enclosure or the lower end enclosure; meanwhile, the heat removing medium enters the shell side from the medium removing inlet and is discharged from the medium removing outlet, so that heat exchange is realized.
The device with the structure has the characteristics and the technical effects that:
firstly, a plurality of axially arranged inner fins are arranged in the tubes, and the inner fins are distributed on the cross section of the tubes at equal angles. The inner fins are in close contact with the catalyst in the tubes, so that reaction heat can be quickly transferred to the tube wall and taken away by a heat removing medium, and meanwhile, reaction materials are divided into a plurality of parts, so that the axial flow (the radial flow is limited) of the reaction materials is enhanced, the catalytic reaction is more uniform, and the temperature of each part of the catalyst is ensured to be uniform to the greatest extent; meanwhile, due to the existence of the inner fins, the heat transfer medium can be used as a heat transfer medium to multiply the comprehensive heat transfer coefficient, and is particularly suitable for chemical reactions with large reaction heat release or strict requirements on reaction temperature change intervals.
In addition, the center and the edge ring of the tube plate are respectively provided with a central circular non-tube distribution area and an edge ring non-tube distribution area; meanwhile, the outer diameter of the circular guide plate corresponds to the inner diameter of the edge circular non-fabric-area, and the inner diameter of the circular guide plate corresponds to the outer diameter of the central circular non-fabric-area. Under the flow guide of the circular guide plates and the annular guide plates which are arranged in a staggered mode at intervals in the shell pass, the heat removing medium mainly flows in the horizontal radial direction in the area corresponding to the pipe distribution area on the cross section, and quickly changes into vertical axial flow in the area corresponding to the pipe non-distribution area, so that a vortex area and a stagnant area are easily formed in the area, and the heat removing medium is a part with poor heat transfer performance. Therefore, the invention is purposefully not provided with the tubes in the non-tube distribution area, the volume utilization rate of the device is not reduced a lot, but the formation of vortex and stagnant flow can be effectively avoided, so that the reaction materials and the heat removing medium form single cross flow, the heat transfer is more uniform and efficient, the shell-side pressure drop is reduced, and the invention is beneficial to the defects.
In conclusion, the structure of the device can realize the uniform flow and the uniform heat exchange of the materials, and control the reaction temperature within a reasonable small range, thereby improving the conversion rate and the selectivity of the hydration reaction.
Preferably, the number of the inner fins is 2-16, and the fin ratio is 1.3-4.0.
Preferably, two ends of each column tube are respectively provided with a spring support, the inner end of each spring support is filled with inert ceramic balls (the height of each spring support covers the spring support), and the inert ceramic balls at the two ends are filled with catalysts.
The spring support is convenient to disassemble and assemble, plays a role of axial support and catalyst fixation together with the inert porcelain ball, and can realize uniform distribution of reaction materials on the cross section of the tube array.
Preferably, the area ratio of the edge annular non-cloth pipe area to the central circular non-cloth pipe area is 1-1.5: 1.
Preferably, one or more pairs of annular channels are arranged on the circumference of the outer side wall of the shell pass cylinder; media withdrawing through holes are uniformly distributed on the circumference of the outer side wall of the shell pass cylinder body corresponding to the annular channel. Wherein:
scheme provided with a pair of annular channels: the two annular channels are respectively arranged on the outer side wall of the shell pass cylinder body close to the top surface and the bottom surface, and the media withdrawing inlet and the media withdrawing outlet are respectively arranged on one annular channel.
Scheme with many pairs of annular passageways: the plurality of pairs of annular channels are sequentially arranged along the axial direction of the shell pass cylinder, and the media withdrawing inlet and the media withdrawing outlet are respectively arranged on one annular channel in each pair; and shell-side intermediate partitions for isolation (for dividing the interior of the shell-side cylinder into a plurality of chambers) are arranged at adjacent pairs of annular channels in the shell-side cylinder.
The medium removing through hole is used as a channel for the heat removing medium to enter the shell side. Because the flow resistance at the medium removing through hole is far larger than the resistance in the annular channel, the medium removing through holes with the same diameter are arranged, and the heat removing medium can uniformly enter the shell pass cylinder along the circumference of the shell pass cylinder.
In addition, the design of many pairs of annular channels, and every heat removal medium's import temperature is the same, how can show the increase heat transfer difference in temperature, effectively improve reaction temperature's controllability.
Preferably, a plurality of medium withdrawing inlets or medium withdrawing outlets are arranged on the outer side of the annular channel along the circumferential direction, and a feeding baffle is arranged between each medium withdrawing inlet and the shell side cylinder.
The design of a plurality of medium withdrawing inlets or medium withdrawing outlets and the arrangement of the feeding baffle plate at the inner side of each medium withdrawing inlet can ensure that the heat withdrawing media are uniformly distributed in the annular channel, thereby realizing the uniform feeding of the medium withdrawing at each part.
Preferably, the feeding baffle is arc-shaped or splayed.
Preferably, distribution plate through holes are uniformly distributed in the areas of the feed distribution plate, which do not correspond to the edge annular non-pipe distribution area and the central circular non-pipe distribution area.
Preferably, the upper end socket and the lower end socket are of a spherical cap end socket type.
The upper and lower end sockets of the device are both spherical end sockets, the spherical end sockets are directly welded with the flange of the shell pass cylinder, and a pipe box straight cylinder section is not arranged, so that the retention time of reaction materials in the end sockets can be reduced, and the occurrence of self-polymerization reaction and side reaction of the materials can be reduced.
In a second aspect, the invention provides a method for preparing 3-hydroxypropanal by acrolein hydration, wherein the hydration reaction is completed by taking the device as a main body, a catalyst is filled in a tube array, a heat removing medium is fed from a medium removing inlet, and a medium removing outlet is used for discharging; feeding the mixed liquid of acrolein and water from a feed inlet, allowing the mixed liquid to flow through the catalyst in the tubes, discharging the mixed liquid from a discharge outlet, and completing hydration reaction at a certain temperature and pressure to obtain the 3-hydroxypropionaldehyde.
The invention only allows a narrow range of reaction temperature range for preparing 3-hydroxypropanal by acrolein hydration, so the device with special structure can ensure that the heat exchange between reaction materials and heat removing medium is more uniform.
Preferably, the mixing ratio of the acrolein to the water is 1:12 to 1:3, and the reaction space velocity is 0.75 to 2.7 hr-1The reaction temperature is 30-80 ℃, and the reaction pressure is 0.1-0.5 MPa.
Compared with the prior art, the invention has the beneficial effects that: the device can meet the hydration reaction characteristics of preparing 3-hydroxy-propionaldehyde by acrolein hydration, and has the advantages of uniform material distribution and heat transfer, high reaction efficiency, high production stability and low energy consumption. The device of the invention is not only suitable for preparing 3-hydroxypropionaldehyde by acrolein hydration, but also suitable for other reactions with similar reaction conditions.
Drawings
FIG. 1 is a front cross-sectional view of an apparatus according to example 1 of the present invention;
FIG. 2 is a cross-sectional view of a tube array in the apparatus of example 1 of the present invention;
FIG. 3 is a longitudinal sectional view of a tube array in an apparatus according to example 1 of the present invention;
FIG. 4 is a top view of a tubesheet in an apparatus according to example 1 of the present invention;
FIG. 5 is a cross-sectional view of a shell-side cylinder and an annular channel in an apparatus according to example 1 of the present invention;
FIG. 6 is a top view of a feed distribution plate in an apparatus according to example 1 of the present invention.
The reference signs are: the device comprises a shell-side cylinder 1, a tube array 2, a circular guide plate 3, an annular guide plate 4, a medium removing inlet 5, a medium removing outlet 6, an upper end enclosure 7, a lower end enclosure 8, a feed inlet 9, a discharge outlet 10, a feed distribution plate 11, an annular channel 12, a tube plate 101, a tube array hole 102, a central circular non-tube distribution area 103, an edge annular non-tube distribution area 104, a medium removing through hole 105, a middle partition plate 106, a feed baffle 107, a spring support 201, an inert ceramic ball 202, an inner fin 203 and a distribution plate through hole 1101.
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
A reaction apparatus for preparing 3-hydroxypropanal by acrolein hydration, as shown in fig. 1, comprising:
the top surface and the bottom surface of the shell side cylinder body 1 are respectively provided with a tube plate 101; the tube plate is provided with tube array holes 102; the central area and the edge area of the tube plate are respectively a central circular non-tube distribution area 103 and an edge annular non-tube distribution area 104 (as shown in fig. 4), and the areas of the central circular non-tube distribution area and the edge annular non-tube distribution area are equal.
And the plurality of tubes 2 are axially arranged in the shell pass cylinder, and two ends of each tube are respectively communicated with tube array holes of the tube plates on the top surface and the bottom surface of the shell pass cylinder. Spring supports 201 (the inner end is in a conical shape) are respectively arranged at two ends of each row tube, the inner ends of the spring supports are filled with inert ceramic balls 202, and catalysts are filled between the inert ceramic balls at the two ends (as shown in fig. 3). In addition, each row of tubes is provided with 6 axially arranged inner fins 203, and the fin ratio is 2.1. The inner fins are distributed at equal angles on the cross section of the tube array (as shown in figure 2). Three groups of multi-point armored thermocouples are arranged in the tube nest to measure the temperature of the catalyst bed layer, two groups of thermocouples are arranged on the shell pass along the axial height, and three thermocouples in each group are uniformly distributed along the circumferential direction of the outer diameter of the cylinder body and are used for measuring the temperature of a heat removing medium (not shown in the thermocouple figure).
And the shell side intermediate partition plate 106 is arranged in the shell side cylinder body and separates the shell side into two chambers. A pair of annular channels 12 (each pair of two annular channels) is respectively arranged on the circumference of the outer side wall of each chamber, and 2 media withdrawing inlets and media withdrawing outlets (the media withdrawing inlets are positioned on one side far away from the feed inlet) are respectively arranged on the two annular channels in each pair; and an arc-shaped feeding baffle 107 is arranged between each media withdrawing inlet and the shell pass cylinder. 24 medium withdrawing through holes 105 (shown in fig. 5) with the same diameter are uniformly distributed on the circumference of the outer side wall of the shell-side cylinder body corresponding to the annular channel.
Each cavity in the shell pass cylinder is respectively provided with 2 circular guide plates 3 and 3 annular guide plates 4 which are axially and alternately arranged in the shell pass cylinder to form a zigzag medium removing flow channel; the outer diameter of the circular guide plate is the same as the inner diameter of the edge annular non-pipe distribution area, and the inner diameter of the annular guide plate is the same as the outer diameter of the central circular non-pipe distribution area.
And the upper end enclosure 7 (in a spherical cap end enclosure type) covers the top of the shell pass cylinder, and is provided with a discharge hole 10.
And the lower end enclosure 8 (in a spherical cap type) is covered at the bottom of the shell pass cylinder body, and a feed inlet 9 is arranged on the lower end enclosure.
And the feeding distribution plate 11 is arranged between the top surface or the bottom surface of the shell pass cylinder and the feeding hole. The feed distribution plate is uniformly distributed with distribution plate through holes 1101 (shown in fig. 6) in the areas of the feed distribution plate not corresponding to the edge annular non-pipe distribution area and the central circular non-pipe distribution area.
A method for preparing 3-hydroxypropionaldehyde by acrolein hydration finishes hydration reaction by taking the device as a main body, and specifically comprises the following steps: filling a catalyst into the tubes, feeding a heat removing medium from a medium removing inlet, and discharging from a medium removing outlet; meanwhile, the mixed liquid of the acrolein and the water is fed from the feed inlet, flows through the catalyst in the tubes and is discharged from the discharge outlet to obtain the 3-hydroxypropionaldehyde. The mixing ratio of the acrolein to the water is 1:9, and the reaction space velocity is 2.1 hr-1The reaction temperature is 65 ℃ and the reaction pressure is 0.3 MPa.
Example 2
Example 2 differs from example 1 in that:
(1) only one pair of annular channels is provided: the two annular channels are respectively arranged on the outer side wall of the shell pass cylinder body close to the top surface and the bottom surface.
(2) Each row of tubes is internally provided with 4 inner fins which are axially arranged, and the finned ratio is 1.7.
(3) The feeding baffle is splayed.
(4) A feed inlet is arranged on the upper seal head; the lower end enclosure is provided with a discharge hole.
(5) The mixing ratio of the acrolein to the water is 1:12, and the reaction space velocity is 2.3hr-1The reaction temperature is 70 ℃ and the reaction pressure is 0.35 MPa.
Example 3
Example 3 differs from example 1 in that:
(1) each row of tubes is internally provided with 8 inner fins which are axially arranged, and the finned ratio is 2.1.
(2) The mixing ratio of the acrolein to the water is 1:4, and the reaction space velocity is 1.8hr-1The reaction temperature is 60 ℃ and the reaction pressure is 0.25 MPa.
The raw materials and equipment used in the invention are common raw materials and equipment in the field if not specified; the methods used in the present invention are conventional in the art unless otherwise specified.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and all simple modifications, alterations and equivalents of the above embodiments according to the technical spirit of the present invention are still within the protection scope of the technical solution of the present invention.
Claims (10)
1. A reaction device for preparing 3-hydroxypropanal by acrolein hydration is characterized by comprising:
the top surface and the bottom surface of the shell side cylinder body (1) are respectively provided with a tube plate (101); the tube plate is provided with tube array holes (102); the central area and the edge area of the tube plate are respectively a central circular non-cloth area (103) and an edge annular non-cloth area (104);
the shell side tube body is provided with a plurality of tube arrays (2) which are axially arranged in the shell side tube body, catalysts are filled in the tube arrays, and two ends of the tube arrays are respectively communicated with tube array holes of tube plates on the top surface and the bottom surface of the shell side tube body; a plurality of axially arranged inner fins (203) are arranged in each row tube, and the inner fins are distributed on the cross section of the row tube at equal angles;
the circular guide plates (3) and the annular guide plates (4) are axially and alternately arranged in the shell pass cylinder to form a zigzag medium removing flow channel; the outer diameter of the circular guide plate corresponds to the inner diameter of the edge annular non-cloth pipe area; the inner diameter of the annular guide plate corresponds to the outer diameter of the central circular non-distribution pipe area;
the media removing inlet (5) and the media removing outlet (6) are directly or indirectly arranged on the outer side wall of the shell side cylinder;
the upper end enclosure (7) is covered on the top of the shell pass cylinder body, and a feed port (9) or a discharge port (10) is formed in the upper end enclosure;
the lower end enclosure (8) is covered at the bottom of the shell pass cylinder body, and a discharge hole or a feed hole is formed in the lower end enclosure;
the feeding distribution plate (11) is arranged between the top surface or the bottom surface of the shell pass cylinder and the feeding hole;
one or more pairs of annular channels (12) are arranged on the circumference of the outer side wall of the shell pass cylinder; media withdrawing through holes (105) are uniformly distributed on the circumference of the outer side wall of the shell pass cylinder body corresponding to the annular channel; a plurality of media withdrawing inlets or media withdrawing outlets are arranged on the outer side of the annular channel along the circumferential direction, and a feeding baffle (107) is arranged between each media withdrawing inlet and the shell side cylinder.
2. The reaction device as claimed in claim 1, wherein each of the column tubes is provided at both ends thereof with a spring holder (201), the spring holder is filled at an inner end thereof with an inert ceramic ball (202), and the inert ceramic balls at both ends are filled with a catalyst.
3. The reaction device according to claim 1, wherein the number of the inner fins is 2 to 16, and the fin ratio is 1.3 to 4.0.
4. The reaction apparatus according to claim 1, wherein the area ratio of the edge annular non-tube distribution area to the central circular non-tube distribution area is 1 to 1.5: 1.
5. The reactor apparatus of claim 1,
scheme provided with a pair of annular channels: the two annular channels are respectively arranged on the outer side wall of the shell pass cylinder body close to the top surface and the bottom surface, and the media withdrawing inlet and the media withdrawing outlet are respectively arranged on one annular channel;
scheme with many pairs of annular passageways: the plurality of pairs of annular channels are sequentially arranged along the axial direction of the shell pass cylinder, and the media withdrawing inlet and the media withdrawing outlet are respectively arranged on one annular channel in each pair; and shell-side intermediate clapboards (106) are arranged at the adjacent and opposite annular channels in the shell-side cylinder body for isolation.
6. The reactor apparatus of claim 1 wherein said feed baffle is arcuate or splayed.
7. The reaction apparatus of claim 1, wherein the feed distribution plate has uniformly distributed distribution plate through holes (1101) in areas of the feed distribution plate not corresponding to the edge annular non-piping area and the central circular non-piping area.
8. The reactor of claim 1, wherein the upper head and the lower head are of a dome head type.
9. A method for preparing 3-hydroxypropanal by acrolein hydration, which is characterized in that the hydration reaction is completed by taking the reaction device as a main body according to any one of claims 1 to 8, a catalyst is filled in a tube array, a heat removing medium is fed from a medium removing inlet, and a medium removing outlet is used for discharging; feeding the mixed liquid of acrolein and water from a feed inlet, allowing the mixed liquid to flow through the catalyst in the tubes, and discharging the mixed liquid from a discharge outlet to obtain the 3-hydroxypropionaldehyde.
10. The method according to claim 9, wherein the mixing ratio of acrolein to water is 1:12 to 1:3, and the reaction space velocity is 0.75 to 2.7 hr-1The reaction temperature is 30-80 ℃, and the reaction pressure is 0.1-0.5 MPa.
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| CN202011613603.0A CN112808178B (en) | 2020-12-30 | 2020-12-30 | Reaction device and method for preparing 3-hydroxypropionaldehyde by acrolein hydration |
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| CN101209402B (en) * | 2006-12-27 | 2011-11-30 | 西安航天华威化工生物工程有限公司 | Shell pass multi-cavity type multi-layer bed fixed bed reactor |
| CN102784596B (en) * | 2012-07-12 | 2014-12-17 | 天津大学 | Shell side structure and shell and tube vinyl acetate synthesis reactor with same |
| CN204093420U (en) * | 2014-08-06 | 2015-01-14 | 中石化南京工程有限公司 | Hydrogenation reactor |
| CN105582859B (en) * | 2014-10-24 | 2019-06-11 | 中国石油化工股份有限公司 | The method of catalytic ammoniation legal system ethanol amine |
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Address after: 311200 29 Chenghu Road, Yaqian Town, Xiaoshan District, Hangzhou City, Zhejiang Province Patentee after: Zhejiang Hengyi Petrochemical Research Institute Co.,Ltd. Patentee after: Zhejiang University Address before: 311200 29 Chenghu Road, Yaqian Town, Xiaoshan District, Hangzhou City, Zhejiang Province Patentee before: ZHEJIANG HENGLAN TECHNOLOGY Co.,Ltd. Patentee before: Zhejiang University |