CN113559792A - Dimethyl ether synthesis reactor and dimethyl ether synthesis process - Google Patents
Dimethyl ether synthesis reactor and dimethyl ether synthesis process Download PDFInfo
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- CN113559792A CN113559792A CN202110801624.3A CN202110801624A CN113559792A CN 113559792 A CN113559792 A CN 113559792A CN 202110801624 A CN202110801624 A CN 202110801624A CN 113559792 A CN113559792 A CN 113559792A
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
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- 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
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- 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
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- C07C41/09—Preparation of ethers by dehydration of compounds containing hydroxy groups
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Abstract
The invention discloses a dimethyl ether synthesis reactor and a dimethyl ether synthesis process, wherein the top of the dimethyl ether synthesis reactor is provided with a methanol feed inlet and a manhole; a first outlet for leading out the catalyst is arranged on the side wall of the lower part of the reactor, and a second outlet for leading out the mixture is arranged at the bottom of the reactor; packing layers containing solid catalysts are arranged in a cavity of the reactor at intervals from top to bottom; the reactor is characterized in that a heat exchange assembly is arranged in a cavity of the reactor, an inlet and an outlet of the heat exchange assembly are respectively communicated with a methanol gas phase and the methanol feed inlet through the side wall of the reactor, and the packing layer is arranged above the first outlet. The heat exchange assembly is arranged in the cavity of the reactor, so that the reactor occupies less space, and has the advantages of low inlet and outlet temperature of the reactor and full utilization of heat.
Description
Technical Field
The invention relates to a preparation process of dimethyl ether, in particular to a dimethyl ether synthesis reactor and a dimethyl ether synthesis process.
Background
Dimethyl ether is also called dimethyl ether, abbreviated as DME. Dimethyl ether is a colorless gas or compressed liquid at atmospheric pressure and has a slight ether flavor. At present, the method for producing dimethyl ether at home and abroad mainly comprises a synthesis gas one-step method and a methanol method, and the methanol method is divided into a methanol gas phase method and a methanol liquid phase method. However, in the existing process for producing dimethyl ether by methanol gas phase method, the temperature of main reactant methanol needs to be raised to about 280 ℃ before entering into the reactor, and a large amount of heat is needed for heating, so that the conversion rate of methanol dehydration reaction is higher. In addition, after the methanol dehydration reaction is carried out in the reactor, due to the reaction heat release, the over-temperature condition occurs in the reactor, and the temperature of the mixture output from the reactor is too high, so that the difficulty of subsequent cooling is greatly increased, meanwhile, the cost is also obviously increased, and the utilization efficiency of heat is low.
Disclosure of Invention
Aiming at the problems, the invention provides the dimethyl ether synthesis reactor and the dimethyl ether synthesis process, which have the advantages of low temperature of the inlet and outlet of the reactor and full utilization of heat.
The technical scheme of the invention is as follows:
a dimethyl ether synthesis reactor is characterized in that the top of the reactor is provided with a methanol feed inlet and a manhole; a first outlet for leading out the catalyst is arranged on the side wall of the lower part of the reactor, and a second outlet for leading out the mixture is arranged at the bottom of the reactor; packing layers containing solid catalysts are arranged in a cavity of the reactor at intervals from top to bottom; the reactor is characterized in that a heat exchange assembly is arranged in a cavity of the reactor, an inlet and an outlet of the heat exchange assembly are respectively communicated with a methanol gas phase and the methanol feed inlet through the side wall of the reactor, and the packing layer is arranged above the first outlet.
The working principle of the technical scheme is as follows: the method comprises the steps of initially introducing a methanol gas phase with the temperature of 250-300 ℃ for a period of time to enable methanol to be subjected to dehydration reaction in a reactor, directly introducing the methanol gas phase with the temperature of 130-160 ℃ into a heat exchange assembly for heat exchange when the temperature in a cavity of the reactor reaches a preset temperature, introducing the methanol gas phase with the temperature of 270-310 ℃ after heat exchange into the reactor from a methanol feed port for general dehydration reaction, directly utilizing the heat release characteristic of the methanol dehydration reaction without initial heating, thereby increasing the temperature of the methanol gas phase entering the methanol feed port, realizing full utilization of heat, saving space, maintaining the temperature in the reactor stable after heat exchange with the heat exchange assembly, and avoiding the over-temperature condition, the temperature of the mixture led out is also reduced, and the cost and the difficulty of subsequent cooling are reduced.
Compared with the prior art, the heat exchange assembly is arranged in the cavity of the reactor, so that the methanol gas phase at 130-160 ℃ needs to be heated to a temperature of 250-300 ℃ by using external heat in the initial stage, the heat released by the methanol dehydration reaction can be used for heating the methanol gas phase in other normal working stages, the temperature entering a methanol feeding port is 270-310 ℃, the temperature amplitude is small, energy is saved, the heat is fully utilized, meanwhile, after the heat exchange assembly exchanges heat, the temperature in the reactor is kept stable, the over-temperature condition is avoided, the temperature of a guided mixture is also reduced, the cost and the difficulty of subsequent cooling are reduced, and the heat exchange assembly is arranged in the reactor, so that the space is obviously saved, and the equipment investment and the maintenance cost are reduced.
In a further technical scheme, the heat exchange device comprises a first heat exchange unit arranged above the first outlet, the first heat exchange unit comprises a plurality of groups of methanol heat exchange tubes arranged from top to bottom at intervals, and the inlet and the outlet of each methanol heat exchange tube are respectively communicated with a methanol gas phase and the methanol feed inlet through the side wall of the reactor.
Through setting up first heat transfer unit in the top of first export, and the packing layer also sets up in the top of first export for after dehydration reaction emits the heat, the methyl alcohol heat exchange tube just can take away the heat at once, when realizing heat make full use of, further avoid appearing the condition of overtemperature in the reactor.
In a further technical scheme, the methanol heat exchange tube is in a spiral winding shape from top to bottom in a cavity of the reactor.
Through setting up the methanol heat exchange tube to spiral winding shape from last to down for the heat transfer is more abundant, and the temperature lifting efficiency in methanol gaseous phase obviously promotes, from last setting down, also avoids the heat accumulation of dehydration reaction simultaneously, further avoids the emergence of the overtemperature conditions.
In a further technical scheme, each group of methanol heat exchange tubes comprises a plurality of branch methanol heat exchange tubes, and inlets of the branch methanol heat exchange tubes are positioned at the same height on the side wall of the reactor.
Each group of methanol heat exchange tubes comprises a plurality of branch methanol heat exchange tubes, so that the flow of the gas phase of the methanol for heat exchange is larger, and the heat is more fully utilized; meanwhile, the inlets of the branch methanol heat exchange tubes are arranged at the same height, so that the temperature amplitude of the methanol at the outlet is small, and the stability is high.
In a further technical scheme, the heat exchange assembly further comprises a second heat exchange unit arranged below the first outlet, and an inlet and an outlet of the second heat exchange unit are respectively communicated with the methanol gas phase and the methanol feed inlet through the side wall of the reactor.
Through set up the second heat transfer unit in the below of first export, can carry out the heat transfer with the methanol gas phase of 130 ℃ -160 ℃ of the downward heat of accumulation of methanol dehydration reaction, further realize thermal make full use of, and effectively promoted the flow that gets into the methanol feed inlet, promoted work efficiency greatly.
In a further technical scheme, the second heat exchange unit comprises a plurality of groups of tubular heat exchangers which are communicated with each other, a plurality of corresponding holes are formed in the tops and the bottoms of the tubular heat exchangers and are communicated with each other through pipelines, and a filtering piece is arranged between the top of the tubular heat exchanger which is positioned at the top and the first outlet.
Through set up a plurality of groups of tubular heat exchangers that communicate each other in second heat transfer unit for 130 ℃ -160 ℃ of methyl alcohol gaseous phase can directly let in tubular heat exchanger, need not the pipeline, and the contact is more abundant, and heat exchange efficiency is higher.
In a further technical scheme, a spray pipe is arranged in a cavity of the reactor, penetrates through the side wall of the reactor and is communicated with a methanol gas phase, and the spray pipe is arranged above at least one layer of the packing layer.
The spraying pipe is arranged in the cavity of the reactor, so that the methanol gas phase at 130-160 ℃ directly enters the reactor, and when the temperature of the reactor is too high, the methanol gas phase can be directly contacted with the reactor for cooling and dehydration reaction, thereby avoiding overtemperature and simultaneously improving the working efficiency.
In a further technical scheme, one end, close to the reactor, of the methanol feed inlet is connected with a distribution pipe, and a plurality of through holes are uniformly distributed on the distribution pipe.
Through set up the distributing pipe at the methyl alcohol feed inlet for the distribution of methyl alcohol is more even, and the operating efficiency further promotes.
Another aspect of the present invention provides a dimethyl ether synthesis process using the reactor as described above, comprising the steps of:
heating to obtain a methanol gas phase with the temperature of 130-160 ℃;
secondary heating to obtain an initial methanol gas phase with the temperature of 250-300 ℃;
introducing the initial methanol gas phase into the methanol feed port and carrying out dehydration reaction under the catalysis of the solid catalyst to continuously release heat;
when the temperature in the chamber of the reactor reaches a preset value, closing the secondary heating;
directly introducing the 130-160 ℃ methanol gas phase into the heat exchange assembly for heat exchange to obtain the methanol with the temperature of 270-310 ℃, and introducing the methanol into the methanol feed inlet for dehydration reaction.
In a further technical scheme, the heat exchange assembly comprises a first heat exchange unit arranged above the first outlet and a second heat exchange unit arranged below the first outlet, the first heat exchange unit comprises a plurality of groups of methanol heat exchange tubes arranged at intervals from top to bottom, the inlets and the outlets of the methanol heat exchange tubes are respectively communicated with a methanol gas phase and the methanol feed inlet through the side wall of the reactor, the second heat exchange unit comprises a plurality of groups of tubular heat exchangers which are mutually communicated, and the inlets and the outlets of the plurality of groups of tubular heat exchangers are respectively communicated with the methanol gas phase and the methanol feed inlet through the side wall of the reactor; after the secondary heating is closed, the methanol gas phase at the temperature of 130-160 ℃ is divided into a first branch and a second branch, the first branch is communicated with the inlet of the methanol heat exchange tube, and the second branch is communicated with the inlets of the plurality of groups of tubular heat exchangers and is communicated with the methanol feed inlet by penetrating through at least two groups of tubular heat exchangers.
The invention has the beneficial effects that:
1. compared with the prior art, the heat exchange assembly is arranged in the cavity of the reactor, so that the methanol gas phase at 130-160 ℃ needs to be heated to a temperature of 250-300 ℃ by using external heat in the initial stage, the heat released by the methanol dehydration reaction can be used in other normal working stages to realize the heating of the methanol gas phase, the temperature entering a methanol feed inlet is 270-310 ℃, the temperature amplitude is small, the energy is saved, the heat is fully utilized, meanwhile, after the heat exchange assembly exchanges heat, the temperature in the reactor is kept stable, the over-temperature condition is avoided, the temperature of a guided-out mixture is also reduced, the cost and the difficulty of subsequent cooling are reduced, and moreover, the heat exchange assembly is arranged in the reactor, the space is obviously saved, and the equipment investment and the maintenance cost are reduced;
2. the first heat exchange unit is arranged above the first outlet, and the filler layer is also arranged above the first outlet, so that after heat is released in the dehydration reaction, the heat can be taken away by the methanol heat exchange tube at once, the heat is fully utilized, and the over-temperature condition in the reactor is further avoided;
3. the methanol heat exchange tube is arranged in a spiral winding shape from top to bottom, so that the heat exchange is more sufficient, the temperature lifting efficiency of the methanol gas phase is obviously improved, meanwhile, the heat accumulation of the dehydration reaction is avoided due to the arrangement from top to bottom, and the over-temperature condition is further avoided;
4. each group of methanol heat exchange tubes comprises a plurality of branch methanol heat exchange tubes, so that the flow of the gas phase of the methanol for heat exchange is larger, and the heat is more fully utilized; meanwhile, the inlets of the branch methanol heat exchange tubes are arranged at the same height, so that the temperature amplitude of the methanol at the outlet is small, and the stability is high;
5. the second heat exchange unit is arranged below the first outlet, so that heat accumulated downwards in the methanol dehydration reaction can exchange heat with the methanol gas phase at 130-160 ℃, the heat is further fully utilized, the flow entering the methanol feed inlet is effectively improved, and the working efficiency is greatly improved;
6. through arranging a plurality of groups of tubular heat exchangers which are communicated with each other in the second heat exchange unit, the methanol gas phase at the temperature of 130-160 ℃ can be directly introduced into the tubular heat exchangers without pipelines, so that the contact is more sufficient, and the heat exchange efficiency is higher;
7. the spraying pipe is arranged in the cavity of the reactor, so that the gas phase of the methanol with the temperature of 130-160 ℃ directly enters the reactor, and when the temperature of the reactor is too high, the gas phase can be directly contacted and cooled and subjected to dehydration reaction, thereby avoiding overtemperature and simultaneously improving the working efficiency;
8. through set up the distributing pipe at the methyl alcohol feed inlet for the distribution of methyl alcohol is more even, and the operating efficiency further promotes.
Drawings
FIG. 1 is a schematic view of the overall structure of a reactor according to an embodiment of the present invention;
FIG. 2 is a process flow diagram of a process for the synthesis of dimethyl ether according to an embodiment of the present invention.
Description of reference numerals:
1-a methanol feed inlet; 2-a first outlet; 3-a second outlet; 4-a filler layer; 5-methanol heat exchange pipe; 6-a filter element; 7-shell-and-tube heat exchanger; 8-a spray pipe; 9-distribution pipes; 10-manhole.
Detailed Description
The embodiments of the present invention will be further described with reference to the accompanying drawings.
Example (b):
as shown in fig. 1, a dimethyl ether synthesis reactor, the top of which is provided with a methanol feed inlet 1 and a manhole 10. The lower side wall of the reactor is provided with a first outlet 2 for leading out the catalyst, and the bottom of the reactor is provided with a second outlet 3 for leading out the mixture. Here, the mixture is dimethyl ether which is a product of dehydration reaction of methanol, unreacted methanol and water, and the like. And a packing layer 4 containing a solid catalyst is arranged in the cavity of the reactor from top to bottom at intervals. For example, the catalyst may be added through the manhole 10. For example, the filler layer 4 can obtain a 340-380 ℃ warm layer, a 370-390 ℃ warm layer and a 380-400 ℃ warm layer from top to bottom in sequence. For example, the solid catalyst may be a catalyst comprising γ -Al2O3The solid catalyst of (4). The reactor is characterized in that a heat exchange assembly is arranged in a cavity of the reactor, an inlet and an outlet of the heat exchange assembly are respectively communicated with a methanol gas phase and the methanol feed inlet 1 through the side wall of the reactor, and the packing layer 4 is arranged above the first outlet 2.
The working principle of the technical scheme is as follows: as shown in fig. 1, initially, introducing a methanol gas phase with a temperature of 250 ℃ to 300 ℃ for a period of time to perform a dehydration reaction of methanol in a reactor, when a chamber of the reactor reaches a preset temperature, directly introducing the methanol gas phase with a temperature of 130 ℃ to 160 ℃ (for example, 140 ℃ and 150 ℃) into a heat exchange component for heat exchange, after heat exchange, the temperature of the methanol can basically reach 270 ℃ to 310 ℃ (for example, 280 ℃, 290 ℃ and 300 ℃), then introducing the methanol gas phase into the reactor from a methanol feed port 1 for a general dehydration reaction, without performing initial heating, but directly utilizing the heat release characteristic of the methanol dehydration reaction, thereby increasing the temperature of the methanol gas phase entering the methanol feed port 1, realizing full utilization of heat, having a small temperature amplitude, and the heat exchange component being arranged inside the reactor, saving space, and simultaneously, after heat exchange with the heat exchange component, the temperature in the reactor is kept stable, the over-temperature condition is avoided, the temperature of the exported mixture is also reduced (for example, the temperature of the exported mixture is usually about 220 ℃), and the cost and the difficulty of subsequent cooling are reduced.
Compared with the prior art, as shown in fig. 1, the heat exchange assembly is arranged in the cavity of the reactor, so that the methanol gas phase at 130-160 ℃ needs to be heated to a temperature of 250-300 ℃ by using external heat in the initial stage, the heat released by the methanol dehydration reaction can be used for heating the methanol gas phase in other normal working stages, the temperature entering the methanol feed port 1 is 270-310 ℃, the temperature amplitude is small, the energy is saved, the heat is fully utilized, meanwhile, the temperature in the reactor is kept stable after the heat exchange with the heat exchange assembly, the overtemperature condition is avoided, the temperature of the led mixture is reduced, the cost and the difficulty of subsequent cooling are reduced, the heat exchange assembly is arranged in the reactor, the space is obviously saved, and the equipment investment and the maintenance cost are reduced.
In another embodiment, the heat exchange device comprises a first heat exchange unit arranged above the first outlet 2, the first heat exchange unit comprises a plurality of groups of methanol heat exchange tubes 5 arranged from top to bottom at intervals, and the inlets and outlets of the methanol heat exchange tubes 5 are respectively communicated with the methanol gas phase and the methanol feed inlet 1 through the side wall of the reactor. For example, a regulating valve can be arranged before the first heat exchange unit to ensure the temperature of the inlet methanol and ensure the stable operation of the reactor. Set up first heat transfer unit through the top at first export 2, and packing layer 4 also sets up in the top of first export 2 for after dehydration reaction released the heat, methyl alcohol heat exchange tube 5 just can take away the heat at once, when realizing heat make full use of, further avoid the condition that appears overtemperature in the reactor.
In a further embodiment, as shown in fig. 1, the methanol heat exchange tubes 5 have a spiral winding shape from top to bottom in the chamber of the reactor. Through setting up methanol heat exchange tube 5 to the spiral winding shape from last to down for the heat transfer is more abundant, and the temperature lifting efficiency in methanol gaseous phase obviously promotes, from last setting down, also avoids the heat accumulation of dehydration reaction simultaneously, further avoids the emergence of the overtemperature conditions.
In another embodiment, each set of methanol heat exchange tubes 5 comprises a plurality of branch methanol heat exchange tubes, and the inlets of the branch methanol heat exchange tubes are located at the same height on the side wall of the reactor. Each group of methanol heat exchange tubes 5 comprises a plurality of branch methanol heat exchange tubes, so that the flow of the methanol gas phase for heat exchange is larger, and the heat utilization is more sufficient; meanwhile, the inlets of the branch methanol heat exchange tubes are arranged at the same height, so that the temperature amplitude of the methanol at the outlet is small, and the stability is high.
In another embodiment, as shown in fig. 1, the heat exchange assembly further comprises a second heat exchange unit disposed below the first outlet 2, and an inlet and an outlet of the second heat exchange unit are respectively communicated with the methanol gas phase and the methanol feed port 1 through a side wall of the reactor. For example, a regulating valve can be arranged before the second heat exchange unit to ensure the temperature of the inlet methanol and ensure the stable operation of the reactor. Through set up second heat transfer unit in the below of first export 2, can carry out the heat transfer with the methanol gas phase of 130 ℃ -160 ℃ of the downward heat of accumulation of methanol dehydration reaction, further realize thermal make full use of, and effectively promoted the flow that gets into methanol feed inlet 1, promoted work efficiency greatly.
In a further embodiment, as shown in fig. 1, the second heat exchange unit comprises a plurality of sets of tubular heat exchangers 6 which are communicated with each other, the top and the bottom of the tubular heat exchangers 6 are provided with a plurality of corresponding holes, the corresponding holes are communicated through a pipeline, and a filter member 7 is arranged between the top of the uppermost set of tubular heat exchangers 6 and the first outlet 2. For example, the filter element 7 may be a dense stainless steel wire mesh to prevent particles such as catalyst from falling down and clogging the second outlet 3 and the tubular heat exchanger 6. Through setting up a plurality of groups tube heat exchanger 6 that communicate each other in second heat exchange unit for 130 ℃ -160 ℃ of methyl alcohol gaseous phase can directly let in tube heat exchanger 6, need not the pipeline, and the contact is more abundant, and heat exchange efficiency is higher.
In a further embodiment, as shown in fig. 1, a shower 8 is arranged in the chamber of the reactor, said shower 8 communicating with the methanol gas phase through the side wall of the reactor, wherein said shower 8 is arranged above at least one layer of said packing layer 4. For example, a pneumatic valve may be provided on the shower to control the opening and closing. The spraying pipe 8 is arranged in the cavity of the reactor, so that the methanol gas phase at 130-160 ℃ directly enters the reactor, and when the temperature of the reactor is too high, the methanol gas phase can be directly contacted with the reactor for cooling and dehydration reaction, thereby avoiding overtemperature temperature runaway and simultaneously improving the working efficiency.
In another embodiment, as shown in fig. 1, one end of the methanol feed port 1 close to the chamber of the reactor is connected with a distribution pipe 9, and a plurality of through holes are uniformly distributed on the distribution pipe 9. Through set up distribution pipe 9 at methyl alcohol feed inlet 1 for the distribution of methyl alcohol is more even, and the operating efficiency further promotes.
Another aspect of the present invention provides a dimethyl ether synthesis process using the reactor as described above, comprising the steps of:
(1) heating to obtain a methanol gas phase with the temperature of 130-160 ℃. Here, taking the methanol gas phase of 130 ℃ to 160 ℃ is a conventional art in the related art, and for example, it may be heated by steam.
(2) And (4) carrying out secondary heating to obtain an initial methanol gas phase with the temperature of 250-300 ℃. For example, the secondary heating may be performed by an electric heater, and the process of the secondary heating is also called the initial start-up.
(3) The initial methanol gas phase was introduced into the methanol feed port 1 and subjected to dehydration reaction by catalysis of the solid catalyst to continue the heat generation.
(4) And when the temperature in the chamber of the reactor reaches a preset value, closing the secondary heating. When the temperature in the chamber of the reactor reaches a preset value, the subsequent heating of the methanol gas phase at 130-160 ℃ can be carried out by utilizing the reaction heat release in the reactor, and secondary heating is not needed.
(5) Directly introducing the 130-160 ℃ methanol gas phase into the heat exchange assembly for heat exchange to obtain the methanol with the temperature of 270-310 ℃, and introducing the methanol into the methanol feed inlet 1 for dehydration reaction.
In another embodiment, the heat exchange assembly comprises a first heat exchange unit arranged above the first outlet 2 and a second heat exchange unit arranged below the first outlet 2, the first heat exchange unit comprises a plurality of groups of methanol heat exchange tubes 5 arranged at intervals from top to bottom, the inlets and outlets of the methanol heat exchange tubes 5 are respectively communicated with the methanol gas phase and the methanol feed inlet 1 through the side wall of the reactor, the second heat exchange unit comprises a plurality of groups of tubular heat exchangers 6 communicated with each other, and the inlets and outlets of the plurality of groups of tubular heat exchangers 6 are respectively communicated with the methanol gas phase and the methanol feed inlet 1 through the side wall of the reactor; after the secondary heating is closed, the methanol gas phase at the temperature of 130-160 ℃ is divided into a first branch and a second branch, the first branch is communicated with the inlet of the methanol heat exchange tube 5, and the second branch is communicated with the inlets of the plurality of groups of tubular heat exchangers 6 and is communicated with the methanol feed port 1 by passing through at least two groups of tubular heat exchangers 6. Through practical with first heat transfer unit and the cooperation of second heat transfer unit, obviously promote work efficiency and output, economic benefits promotes to be showing.
The above-mentioned embodiments only express the specific embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the present invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention.
Claims (10)
1. A dimethyl ether synthesis reactor is characterized in that the top of the reactor is provided with a methanol feed inlet and a manhole; a first outlet for leading out the catalyst is arranged on the side wall of the lower part of the reactor, and a second outlet for leading out the mixture is arranged at the bottom of the reactor; packing layers containing solid catalysts are arranged in a cavity of the reactor at intervals from top to bottom; the reactor is characterized in that a heat exchange assembly is arranged in a cavity of the reactor, an inlet and an outlet of the heat exchange assembly are respectively communicated with a methanol gas phase and the methanol feed inlet through the side wall of the reactor, and the packing layer is arranged above the first outlet.
2. The dimethyl ether synthesis reactor according to claim 1, wherein the heat exchange device comprises a first heat exchange unit arranged above the first outlet, the first heat exchange unit comprises a plurality of groups of methanol heat exchange tubes arranged from top to bottom at intervals, and inlets and outlets of the methanol heat exchange tubes are respectively communicated with the methanol gas phase and the methanol feed inlet through the side wall of the reactor.
3. The dimethyl ether synthesis reactor according to claim 2, wherein the methanol heat exchange tube has a spiral winding shape from top to bottom in the chamber of the reactor.
4. The dimethyl ether synthesis reactor according to claim 2, wherein each group of methanol heat exchange tubes comprises a plurality of branch methanol heat exchange tubes, and inlets of the branch methanol heat exchange tubes are positioned at the same height on the side wall of the reactor.
5. The dimethyl ether synthesis reactor according to claim 2, wherein the heat exchange assembly further comprises a second heat exchange unit disposed below the first outlet, and an inlet and an outlet of the second heat exchange unit are respectively communicated with the methanol gas phase and the methanol feed port through a side wall of the reactor.
6. A dimethyl ether synthesis reactor according to claim 5, wherein the second heat exchange unit comprises a plurality of sets of tubular heat exchangers which are communicated with each other, the top and the bottom of the tubular heat exchangers are provided with a plurality of corresponding holes, the corresponding holes are communicated through pipelines, and a filter member is arranged between the top of the tubular heat exchanger of the uppermost set and the first outlet.
7. The dimethyl ether synthesis reactor according to claim 2, wherein a spray pipe is arranged in the cavity of the reactor, the spray pipe penetrates through the side wall of the reactor and is communicated with the methanol gas phase, and the spray pipe is arranged above at least one layer of the packing layer.
8. The dimethyl ether synthesis reactor according to claim 1, wherein one end of the methanol feed inlet, which is close to the reactor chamber, is connected with a distribution pipe, and a plurality of through holes are uniformly distributed on the distribution pipe.
9. A process for the synthesis of dimethyl ether using a reactor according to any one of claims 1 to 8, comprising the steps of:
heating to obtain a methanol gas phase with the temperature of 130-160 ℃;
secondary heating to obtain an initial methanol gas phase with the temperature of 250-300 ℃;
introducing the initial methanol gas phase into the methanol feed port and carrying out dehydration reaction under the catalysis of the solid catalyst to continuously release heat;
when the temperature in the chamber of the reactor reaches a preset value, closing the secondary heating;
directly introducing the 130-160 ℃ methanol gas phase into the heat exchange assembly for heat exchange to obtain the methanol with the temperature of 270-310 ℃, and introducing the methanol into the methanol feed inlet for dehydration reaction.
10. The dimethyl ether synthesis process according to claim 9, wherein the heat exchange assembly comprises a first heat exchange unit arranged above the first outlet and a second heat exchange unit arranged below the first outlet, the first heat exchange unit comprises a plurality of groups of methanol heat exchange tubes arranged at intervals from top to bottom, the inlets and outlets of the methanol heat exchange tubes are respectively communicated with the methanol gas phase and the methanol feed inlet through the side wall of the reactor, the second heat exchange unit comprises a plurality of groups of tubular heat exchangers which are mutually communicated, and the inlets and outlets of the plurality of groups of tubular heat exchangers are respectively communicated with the methanol gas phase and the methanol feed inlet through the side wall of the reactor; after the secondary heating is closed, the methanol gas phase at the temperature of 130-160 ℃ is divided into a first branch and a second branch, the first branch is communicated with the inlet of the methanol heat exchange tube, and the second branch is communicated with the inlets of the plurality of groups of tubular heat exchangers and is communicated with the methanol feed inlet by penetrating through at least two groups of tubular heat exchangers.
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| CN114160053A (en) * | 2022-02-14 | 2022-03-11 | 龙口市化工厂 | Sulfuryl fluoride reaction device |
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| CN101838185A (en) * | 2009-03-20 | 2010-09-22 | 上海吴泾化工有限公司 | Dehydration reactor |
| CN205095758U (en) * | 2015-09-06 | 2016-03-23 | 上海河图工程股份有限公司 | Methanol to propylene's fixed bed reactor |
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| CN101244986A (en) * | 2008-01-14 | 2008-08-20 | 宁波远东化工集团有限公司 | Dimethyl ether reactor |
| CN101838185A (en) * | 2009-03-20 | 2010-09-22 | 上海吴泾化工有限公司 | Dehydration reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114160053A (en) * | 2022-02-14 | 2022-03-11 | 龙口市化工厂 | Sulfuryl fluoride reaction device |
| CN114160053B (en) * | 2022-02-14 | 2022-05-31 | 龙口市化工厂 | Sulfuryl fluoride reaction device |
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