CN2900522Y - Heat exchanging type dimethyl ether synthetic tower - Google Patents
Heat exchanging type dimethyl ether synthetic tower Download PDFInfo
- Publication number
- CN2900522Y CN2900522Y CN 200620073618 CN200620073618U CN2900522Y CN 2900522 Y CN2900522 Y CN 2900522Y CN 200620073618 CN200620073618 CN 200620073618 CN 200620073618 U CN200620073618 U CN 200620073618U CN 2900522 Y CN2900522 Y CN 2900522Y
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- CN
- China
- Prior art keywords
- shell
- tube
- synthetic tower
- end socket
- packing layer
- 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.)
- Expired - Lifetime
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Abstract
This utility model discloses a synthesized tower which is provided with a coil pipe heat exchanger in a shell with easily controlled bed layer temperatures and highly efficient cubage availability ratio for solving the problems of complicated conformation, low transforming rate and low energy comprehensive availability ratio of the reaction heat removing equipment of a carbinol and bi-carbinol converter, which comprises a shell (4) and activators (7) which are filled in the shell (4) whose both ends respectively connect with sealing terminals (2). One sealing terminal (2) is provided with an air inlet (e), and the other is provided with an air outlet (f). A scour-proof device (9) is arranged on one end close to the air inlet (e) in the shell (4), and a material filling layer (3) is arranged on one end close to the air outlet (f), and is characterized in that the shell (4) between the scour-proof device (9) and the material filling layer (3) is provided with a heat exchanger (6) which connects with corresponding a steam inlet tube and a steam outlet tube with simple conformation and high transforming rate.
Description
Technical field
The utility model relates to a kind of chemical industry equipment, especially a kind of dme synthetic tower, specifically a kind of heat exchange type dme synthetic tower.
Background technology
As everyone knows, for the methyl alcohol depressed is synthetic, synthetic this class exothermic catalytic reaction of dme adding, in reaction process, constantly can emits reaction heat reaction bed temperature is improved.In order to improve the efficient of reactor, must remove these reaction heat and reduce temperature of reaction.At present, in industrial reactor, adopt the shell pipe type reactor mostly, loading catalyst in the pipe, tube side is made in reaction leave with rage, and shell side adopts the boiling water shifting heat to steam, and also has the adiabatic cold shocking type of employing or cold-tube type reactor to reduce temperature of reaction in addition.Former structure is simple and reliable, and is easy to adjust, but transformation efficiency and throughput are lower, and latter's bed temperature distributes more satisfactory, structure is also comparatively simple, and volumetric efficiency is higher, but complex structure, the manufacturing cost height, maintenance is inconvenient, and the two is all not ideal in the comprehensive utilization of the energy.
Summary of the invention
The purpose of this utility model be at existing methyl alcohol, that dimethanol synthetic tower reaction heat is removed the complex structure, the transformation efficiency that exist in the equipment is low, the problem that the comprehensive utilization of energy rate is not high, design and a kind ofly can make bed temperature distribute preferable and be easy to control, capacity utilization is higher, can also utilize reaction heat that the methanol steam heating is made it to reach into the tower temperature, thereby reach self thermally equilibrated existing shell pipe type reactor advantage, can further improve the heat exchange type dme synthetic tower of transformation efficiency again.
The technical solution of the utility model is:
A kind of heat exchange type dme synthetic tower, comprise shell 4, catalyzer 7, two ends of shell 4 are connected with end socket 2 respectively, one of them end socket 2 is provided with inlet mouth e, another end socket 2 is provided with air outlet f, in the end socket 2 that is provided with inlet mouth e, be provided with the erosion control device 9 that links to each other with inlet mouth e, the bottom of erosion control device 9 is provided with packing layer 8, be provided with packing layer 3 near in the end of air outlet f, it is characterized in that in the shell 4 between last packing layer 8 and following packing layer 3 interchanger 6 being installed, interchanger 6 all is connected with corresponding steam steam inlet pipe and steam outlet pipe; Catalyzer 7 is seated in the shell 4 between packing layer 8 and the following packing layer 3.
The utility model has also further been taked following technical measures:
Described interchanger 6 can be made up of some groups of tube exchangers, every group of tube exchanger is made up of some circle concentric annular coil pipe 6-1, coil pipe frame 6-2 and annular bottom plate 6-3, the inwall of annular bottom plate 6-3 and shell 4 is weldingly connected, coil pipe frame 6-2 is welded on the annular bottom plate 6-3, and ring-type coil pipe 6-1 is positioned in the shell 4 by coil pipe frame 6-2; In the gap of ring-type coil pipe 6-1, be filled with catalyzer 7.
Described interchanger 6 also can be made up of some groups of shell and tube heat exchanger, every group of shell and tube heat exchanger by the some heat transfer tube 5-1 that arrange vertically, reach the tube sheet 5-3 parallel with the vertical traverse baffle 5-2 of heat transfer tube 5-1 and form with traverse baffle 5-2, the inwall of tube sheet 5-3 and shell 4 is weldingly connected, traverse baffle 5-2 is between tube sheet 5-3, heat transfer tube 5-1 is between tube sheet 5-3 and pass traverse baffle 5-2, is filled with catalyzer 7 in the space of shell and tube heat exchanger.
The ratio heat transfer area of described interchanger 6 is 11～15 meters
2/ rice
3Catalyzer.
Described shell 4 is made up of plurality of sections, links to each other by joint flange 5 between section and the section and between section and the end socket.
The collector 1 that communicates with air outlet f is installed in the end socket that is provided with air outlet f.
Discharge tube a is installed on the end socket that is provided with air outlet f.
The utlity model has following advantage:
1, has very high transformation efficiency (〉=70%), far above adiabatic cold shocking type, shell pipe type and cold-tube type synthetic tower.
2, the bed temperature distribution is preferable, and volumetric efficiency and throughput are higher.
3, the inlet circulating flow rate is little, has significantly reduced power consumption.
4, can will enter methanol steam direct heating in the axial multilayer heat exchange group axial arranged of synthetic tower continuously, thereby improve heat utilization ratio greatly along tower body.
5, stable operation is easy to regulating and controlling, easy to loading and unloading, reliable in structure.
6, applied range not only can be used for methyl alcohol, dimethanol synthetic tower, also can be used for similar synthetic tower.
Description of drawings
Fig. 1 is one of structural representation of the present utility model.
Fig. 2 is two of a structural representation of the present utility model.
Embodiment
Following structure drawings and Examples are further described the utility model.
Embodiment one.
As shown in Figure 1.
A kind of heat exchange type dme synthetic tower is filled with granular aluminium oxide catalyst 2.2m
3, diameter can be DN1000, advances tower tolerance 1900kg/h, inlet tower gas CH3OH 99～99.9%, and pressure 1.05MPa, temperature of reaction～270 ℃, transformation efficiency reaches 73%, produces 12000 tons of dme per year.
This synthetic tower is mainly by collector 1, on, following two end sockets 2, following packing layer 3, shell 4, joint flange 5, some groups (can be 4 groups, but be not limited only to 4 groups) axial tube exchanger 6, catalyzer 7, last packing layer 8, erosion control device 9 is formed, shell 4 by plurality of sections (as 4 sections, but be not limited only to 4 sections) linking to each other forms, between section and the section, the section with end socket between all link to each other by joint flange 5, wherein every group of axial tube exchanger 6 is again by a few concentric annular coil pipes 6-1, coil pipe frame 6-2, ring-like base plate 6-3 constitutes, concentric annular coil pipe 6-1 is fixed on the coil pipe frame 6-2 by certain axial spacing, steam inlet pipe b1～the b4 that links to each other with concentric annular coil pipe 6-1, the end of steam outlet pipe c1～c4 is welded on the shell 4, also adopts between the inwall of ring-like base plate 6-3 and shell 4 and the coil pipe frame 6-2 to be weldingly connected.Be welded with steam inlet pipe e, erosion control device 9 on upper cover 2, lower cover is welded with steam outlet pipe f, collector 1, discharge tube a.In the gap of catalyst loading between upper and lower packing layer 8,3 and concentric annular coil pipe 6-1.
Gas is entered by steam inlet pipe e, behind erosion control device 9 and last packing layer 8, enter Catalytic Layer 7, gas flows and the generation strong exothermal reaction from top to bottom at catalyst layer, reaction heat respectively by in the axial multilayer set of heat exchange tubes of mobile from bottom to top and the methanol steam that will go into tower remove, reacted gas leaves the following packing layer 3 that beds 7 enters the bottom, and f goes out synthetic tower by steam outlet pipe.
Methanol steam enters axial tube exchanger 6 by steam inlet pipe b1～b4 is reverse, wriggles from bottom to top and flows, and goes out from steam outlet pipe c1-c4 and removes bed reaction heat in the beds 7, and methanol steam is heated to into the required temperature of tower.
Filler 3 is seated in the upper and lower position (as Fig. 1) of synthetic tower, and the assembling of pelleted catalyst and synthetic tower is carried out synchronously, makes it be filled in upper and lower packing layer 8,3 uniformly and axially in the gap between the tube exchanger 6.
During concrete enforcement, the visual tower height of group number of the axial tube exchanger of installing in each synthetic tower shell 46 is determined, the axial number of turns of concentric annular coil pipe 6-1 in every group can be determined as required that also their quantity is not subjected to the restriction of present embodiment.
Embodiment two.
As shown in Figure 2.
A kind of heat exchange type dme synthetic tower, filling granular aluminium oxide catalyst 2.2m
3, diameter can be DN1000, advances tower tolerance 1900kg/h, inlet tower gas CH
3OH 98～99.8%, pressure 1.05MPa, and temperature of reaction～270 ℃, transformation efficiency reaches 73%, produces 12000 tons of dme per year.
Above-mentioned synthetic tower is mainly by collector 1, end socket 2, following packing layer 3, joint flange 5, some groups (as shown are 4 groups, but be not limited only to 4 groups) shell and tube heat exchanger 6, shell 4, catalyzer 7, last packing layer 8, erosion control device 9 is formed, wherein every group of shell and tube heat exchanger 6 is again by the many heat transfer tube 5-1 that arrange vertically, with vertical traverse baffle 5-2 of heat transfer tube 5-1 and the tube sheet 5-3 composition parallel with traverse baffle 5-2, the inwall of tube sheet 5-3 and shell 4 is weldingly connected, traverse baffle 5-2 is between tube sheet 5-3, heat transfer tube 5-1 is between tube sheet 5-3 and pass traverse baffle 5-2, is filled with catalyzer 7 in the space of shell and tube heat exchanger 6.Heat transfer tube 5-1 is arranged in the tube sheet 5-3 by certain spacing, adopts welding between heat transfer tube 5-1 and tube sheet 5-3 and tube sheet 5-3 and the housing 4.Be welded with inlet mouth e on upper cover 2, inlet mouth e is connected with erosion control device 9, is welded with air outlet f on the lower cover 2, and air outlet f is connected with collector 1, also is connected with discharge tube a on the lower cover 2.In the gap and the gap between the shell and tube heat exchanger 6 of catalyst loading between upper and lower packing layer 8,3.Shell 4 can be made up of plurality of sections (can be 4 sections, but be not limited only to 4 sections), between section and the section, section with end socket between all link to each other by joint flange 5.
Gas is entered by inlet mouth e, behind erosion control device 9 and top packing layer 8, enter Catalytic Layer 7, gas flows and the generation strong exothermal reaction from top to bottom at catalyst layer, reaction heat is respectively via behind the mobile heat transfer tube methanol steam being removed from bottom to top, reacted gas leaves the packing layer 3 that beds 7 enters the bottom, flows out synthetic tower by steam outlet f.
Methanol steam is by reverse each shell and tube heat exchanger 6 that enters of steam inlet pipe b1～b4, and baffling flows from bottom to top, removes the bed reaction heat in the beds 7, and flows out from steam outlet pipe (c1-c4), and methanol steam is heated to into the required temperature of tower.
Filler 3,8 is seated in the upper and lower position of equipment (seeing figure), and pelleted catalyst filling can be carried out synchronously with device assembles, and it is filled in the gap between upper and lower filler and the shell and tube heat exchanger 6 uniformly.
During concrete enforcement, the visual tower height of group number of the axial row tubular heat exchanger of installing in each synthetic tower housing 46 determined, the quantity of the heat transfer tube 5-1 in every group can be determined as required that also their quantity is not subjected to the restriction of present embodiment.
It is all same as the prior art that the utility model does not relate to part.
Claims (7)
1, a kind of heat exchange type dme synthetic tower, comprise shell (4), catalyzer (7), two ends of shell (4) are connected with end socket (2) respectively, one of them end socket (2) is provided with inlet mouth (e), another end socket (2) is provided with air outlet (f), in the end socket that is provided with inlet mouth (e) (2), be provided with the erosion control device (9) that links to each other with inlet mouth (e), the bottom of erosion control device (9) is provided with packing layer (8), be provided with packing layer (3) near in the end of air outlet (f), it is characterized in that the shell (4) between packing layer on being arranged in (8) and the following packing layer (3) is equipped with interchanger (6), interchanger (6) is connected with corresponding steam steam inlet pipe and steam outlet pipe; Catalyzer (7) is seated in the shell (4) between packing layer (8) and the following packing layer (3).
2, heat exchange type dme synthetic tower according to claim 1, it is characterized in that described interchanger (6) is made up of some groups of tube exchangers, every group of tube exchanger is made up of some circle concentric annular coil pipes (6-1), coil pipe frame (6-2) and annular bottom plate (6-3), annular bottom plate (6-3) is weldingly connected with the inwall of shell (4), coil pipe frame (6-2) is welded on the annular bottom plate (6-3), and ring-type coil pipe (6-1) is positioned in the shell (4) by coil pipe frame (6-2); In the gap of ring-type coil pipe (6-1), be filled with catalyzer (7).
3, heat exchange type dme synthetic tower according to claim 1, it is characterized in that described interchanger (6) is made up of some groups of shell and tube heat exchanger, every group of shell and tube heat exchanger is by the some heat transfer tubes of arranging vertically (5-1), with vertical traverse baffle of heat transfer tube (5-1) (5-2) and tube sheet (5-3) composition parallel with traverse baffle (5-2), tube sheet (5-3) is weldingly connected with the inwall of shell (4), traverse baffle (5-2) is positioned between the tube sheet (5-3), heat transfer tube (5-1) is positioned between the tube sheet (5-3) and passes traverse baffle (5-2), is filled with catalyzer (7) in the space of shell and tube heat exchanger.
4, heat exchange type dme synthetic tower according to claim 1 is characterized in that the ratio heat transfer area of described interchanger (6) is 11～15 meters
2/ rice
3Catalyzer.
5, heat exchange type dme synthetic tower according to claim 1 is characterized in that described shell (4) is made up of plurality of sections, between section and the section and section with end socket between link to each other by joint flange (5).
6, heat exchange type dme synthetic tower according to claim 1 is characterized in that being equipped with the collector (1) that communicates with air outlet (f) in the end socket that is provided with air outlet (f).
7, heat exchange type dme synthetic tower according to claim 1 is characterized in that being equipped with discharge tube (a) on the end socket that is provided with air outlet (f).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620073618 CN2900522Y (en) | 2006-06-08 | 2006-06-08 | Heat exchanging type dimethyl ether synthetic tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620073618 CN2900522Y (en) | 2006-06-08 | 2006-06-08 | Heat exchanging type dimethyl ether synthetic tower |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2900522Y true CN2900522Y (en) | 2007-05-16 |
Family
ID=38084684
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200620073618 Expired - Lifetime CN2900522Y (en) | 2006-06-08 | 2006-06-08 | Heat exchanging type dimethyl ether synthetic tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2900522Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101480592B (en) * | 2008-01-12 | 2012-01-11 | 杭州林达化工技术工程有限公司 | Fixed bed composite reaction equipment |
| CN113559792A (en) * | 2021-07-15 | 2021-10-29 | 成都众奇化工有限公司 | Dimethyl ether synthesis reactor and dimethyl ether synthesis process |
-
2006
- 2006-06-08 CN CN 200620073618 patent/CN2900522Y/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101480592B (en) * | 2008-01-12 | 2012-01-11 | 杭州林达化工技术工程有限公司 | Fixed bed composite reaction equipment |
| CN113559792A (en) * | 2021-07-15 | 2021-10-29 | 成都众奇化工有限公司 | Dimethyl ether synthesis reactor and dimethyl ether synthesis process |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Tianjin Chenchuang Environment Engineering Science & Technology Co., Ltd. Assignor: Nanjing Dahua Chemical Equipment Co. Ltd. Contract fulfillment period: 2009.3.30 to 2014.3.30 Contract record no.: 2009120000071 Denomination of utility model: Heat exchanging type dimethyl ether synthetic tower Granted publication date: 20070516 License type: Exclusive license Record date: 20090630 |
|
| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2009.3.30 TO 2014.3.30; CHANGE OF CONTRACT Name of requester: TIANJIN CHENCHUANG ENVIRONMENT ENGINEERING SCIENCE Effective date: 20090630 |
|
| CX01 | Expiry of patent term |
Granted publication date: 20070516 |
|
| EXPY | Termination of patent right or utility model |