CN201288156Y - Novel two-stage inner-heat exchange dimethyl ether reactor - Google Patents
Novel two-stage inner-heat exchange dimethyl ether reactor Download PDFInfo
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- CN201288156Y CN201288156Y CNU2008200631704U CN200820063170U CN201288156Y CN 201288156 Y CN201288156 Y CN 201288156Y CN U2008200631704 U CNU2008200631704 U CN U2008200631704U CN 200820063170 U CN200820063170 U CN 200820063170U CN 201288156 Y CN201288156 Y CN 201288156Y
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Abstract
A new two-section inner-heat-transfer dimethyl ether reactor for dimethyl ether fabrication technology of methanol gas phase catalytic dehydration, which belongs to a field relating to reactors for filling catalyst. The new two-section inner-heat-transfer dimethyl ether reactor can remove heat of reaction in time, which avoids partial temperature excess or over temperature of reaction gas of bed, thus the reactor is stable to operate, thereby controlling and reducing side reactions. The new two-section inner-heat-transfer dimethyl ether reactor can reduce temperature of methanol entering into the reactor in order to rationalize heat utilization of the reaction system. A section of the new two-section inner-heat-transfer dimethyl ether reactor adopts a radial bed structure, thereby greatly reducing resistance force and more adapting to large-scale units.
Description
Affiliated technical field
The utility model relates to reactor packed with catalyst.Be specifically related to be used for novel two sections internal heat exchange type dimethyl ether reactors of methanol vapor phase catalytic dehydration preparing dimethy ether technology.
Background technology
Dme (Dimethyl Ether, abbreviation DME) is a kind of colourless, nontoxic gas under the normal temperature and pressure state, can compressedly be liquid.Be important Organic Chemicals and chemical intermediate, can be used for industries such as aerosol, refrigeration agent, alkylating agent, pharmacy, makeup, dyestuff.Dme is harmless to atmospheric ozone layer, very easily degrades at the atmosphere convection layer, is the favorable substitutes of fluorochlorohydrocarbon.
Dme is an oxygenatedchemicals, sufficient combustion, does not analyse charcoal, almost noresidue and exhaust emission, is the clean fuel that is only second to hydrogen.Substitute as vehicle fuel (especially diesel oil) and civil liquefied gas fuel faces good market outlook, the title of " clean environment-friendly fuel is arranged ".
The main method of producing dme at present both at home and abroad is that methanol steam is at filling γ-Al
2O
3Generate dme Deng carrying out dehydration reaction in the dimethyl ether reactor of catalyzer.The structure formation of dimethyl ether reactor has: multistage cold shock formula reactor; Tubulation heat exchanging type uniform-temperature reactor etc.
The production technique that adopts multistage cold shock formula reactor to produce dme is that the methanol steam segmentation enters in the multistage cold shock formula reactor, the raw material cold methanol vapor absorption the preceding paragraph reaction heat that utilizes multistage to enter makes the unlikely significantly rising of reactor temperature, the amount of utilizing control to enter the material benzenemethanol of every section beds is controlled the response intensity of each section simultaneously, reaction can be controlled, and temperature can be stabilized in certain limit.But multistage cold shock formula reactor has inevitable defective: in multistage cold shock formula reactor, the fluctuation of reaction bed temperature indention, temperature of lower at every section beds is higher, the inevitable overheating problem that takes place, this exactly every section higher overheating problem of catalyzer lower floor temperature, not only cause overtemperature zone catalyst damage that catalyst performance is descended and lifetime, but also cause the increased response of paying in comparatively high temps and overtemperature zone.Pair reaction that causes by product to increase mainly just occurs in the overtemperature zone of every section catalyzer lower floor.Owing to pay reaction, increased raw material consumption, and increased the difficulty of follow-up sepn process.
In view of the defective that multistage cold shock formula reactor exists, tubulation heat exchanging type uniform-temperature reactor etc. occur in succession.But still there are deficiencies such as cost height, bed resistance be big in these reactors.
Summary of the invention
The utility model provides a kind of novel two sections internal heat exchange type dimethyl ether reactors that are used for methanol vapor phase catalytic dehydration preparing dimethy ether technology.It is stronger thermopositive reaction that methanol dehydration generates dme, and novel two sections internal heat exchange type dimethyl ether reactors that the utility model provides can guarantee reaction process temperature substantially constant, does not make it that local overheating takes place and controls and reduce and pay reaction; Can in time shift out reaction heat and utilization rationally, accomplish not need additionally to provide the external heat source (middle pressure saturation steam or heat-conducting oil furnace) that gas-phase methanol is heated to feeding temperature (about 250 ℃); Can guarantee stably manufactured, reduce methanol consumption, save power consumption, simplify flow process; And being specially adapted to device maximizes.
It is as follows that the utility model addresses the above problem the technical scheme of being taked:
1, novel two sections internal heat exchange type dimethyl ether reactors described in the utility model are a vertical bearing housing, be provided with two-stage catalytic agent bed in the housing: upper bed layer central authorities are tubular heat exchange, establish coiled pipe cooler in the lower bed layer, material benzenemethanol gas is after twice heat exchange, after temperature rises to about 250 ℃, pass catalyst bed and enter heat exchanger shell pass from upper bed layer import radial distribution device, after the heat exchange cooling, enter the lower section catalyst bed, the heat that reacts of leaving the bed is removed by the bed inner coil pipe, and uses the bed gas temperature less than 310 ℃.
2, novel two sections internal heat exchange type dimethyl ether reactors described in the utility model, it is characterized in that: the tubular heat exchange of upper bed layer central authorities is tubular heat exchanges that freely stretch, and tube side is a material benzenemethanol gas, and shell side is through the reacted reaction gas of catalyzer upper bed layer.
3, novel two sections internal heat exchange type dimethyl ether reactors described in the utility model is characterized in that: be provided with coiled pipe cooler in the beds of leaving the bed, purpose is in time to remove reaction heat, and coiled pipe cooler can be one or more layers.
4, novel two sections internal heat exchange type dimethyl ether reactors described in the utility model is characterized in that: no matter go to bed or leave the bed, all can be designed to radial bed or axial bed as required; Direction of flow both can also can move from the outside laminar flow of central authorities from outer course central flows.
5, novel two sections internal heat exchange type dimethyl ether reactors described in the utility model, it is characterized in that: the catalyst bed number of layers is calculated according to chemical technique and scheme relatively is provided with the back flexibly, can be a bed, two beds or more, also can be to be all bed structure or to be all down bed structure.
6, novel two sections internal heat exchange type dimethyl ether reactors described in the utility model, the refractory ball at two kinds of different sizes of bottom filling with better supporting catalyst, does not need support grid, and helps drawing off of catalyzer.
The utility model adopts such structure formation to make this reacting appliance that following advantage be arranged:
---the catalyzer upper bed layer adopts radially reaction bed, has strengthened the circulation area of reactant gases, can make that the reaction bed thermograde changes steadily, bed is difficult for overtemperature, has reduced a pair reaction; Bed resistance is fallen significantly reduce, save energy consumption.
---the catalyzer lower bed layer adopts axial reaction bed, and built-in one or more layers coil heat exchanger can in time pass to reaction heat the material benzenemethanol gas in the coil pipe, keeps bed temperature and changes not quite, is difficult for overtemperature, has reduced a pair reaction.
---owing to strengthen this inside reactor heat exchange effect, utilization of Heat of Reaction is reasonable, not needing additionally provides the external heat source (middle pressure saturation steam or heat-conducting oil furnace) that gas-phase methanol is heated to feeding temperature (about 250 ℃), can make process simplification, saves the general facilities investment, significantly reduce energy consumption.
---the catalyst bed number of layers is calculated according to chemical technique and scheme relatively is provided with the back flexibly, that is: can be a bed, two beds or more, also can be to be all bed structure or to be all down bed structure.
---be specially adapted to device and maximize.
Description of drawings
Accompanying drawing is the dimethyl ether reactor that is used for the novel built-in heat exchanger of methanol vapor phase catalytic dehydration preparing dimethy ether technology.
1, the piece number explanation
Piece number 1: central array tube heat-exchanger
Piece number 2: catalyzer upper bed layer
Piece number 3: catalyzer lower bed layer
Piece number 4: pneumatic outlet collector
Piece number 5: cylindrical shell
2, mouth of pipe explanation
N1: raw material gaseous methanol import
N2: reaction gas outlet
N3: catalyzer discharge opening
N4: manhole
N5: manhole
Embodiment
Embodiment 1: the novel two sections internal heat exchange type dimethyl ether reactors that are used for methanol vapor phase catalytic dehydration preparing dimethy ether device (600,000 tons/year)
Reactor diameter Φ 3400, height overall H=14400.Built-in tubular heat exchange diameter of phi 1100, height overall H=4400.Loading catalyst 60M
3
Reaction pressure 1.0-1.2MPa.
80-150 ℃ of raw material gaseous methanol inlet temperatures, behind the tubular heat exchange tube side that coil heat exchanger that catalyzer is left the bed and catalyzer are gone to bed, temperature reaches about 250 ℃, enter catalyzer upper bed layer, tubular heat exchange shell side, catalyzer lower bed layer successively, up to the gas reactor outlet, this moment, temperature was about 310 ℃.
The per pass conversion of material benzenemethanol is greater than 80%, and selectivity is more than 99%.
Claims (3)
1, a kind of novel two sections internal heat exchange type dimethyl ether reactors that are used for methanol vapor phase catalytic dehydration preparing dimethy ether technology, it is characterized in that: these novel two sections internal heat exchange type dimethyl ether reactors are a vertical bearing housing, be provided with two-stage catalytic agent bed in the housing, upper bed layer central authorities are tubular heat exchange, establish coiled pipe cooler in the lower bed layer, material benzenemethanol gas is through twice heat exchange, after temperature rises to about 250 ℃, pass catalyst bed and enter heat exchanger shell pass from upper bed layer import radial distribution device, enter the lower section catalyst bed after the heat exchange cooling, the heat of the reaction of leaving the bed is removed by the bed inner coil pipe, and uses the bed gas temperature less than 310 ℃.
2, novel two sections internal heat exchange type dimethyl ether reactors according to claim 1, it is characterized in that: the tubular heat exchange of upper bed layer central authorities is tubular heat exchanges that freely stretch, and tube side is a material benzenemethanol gas, and shell side is through the reacted reaction gas of catalyzer upper bed layer.
3, novel two sections internal heat exchange type dimethyl ether reactors according to claim 1 is characterized in that: be provided with coiled pipe cooler in the beds of leaving the bed, coiled pipe cooler can be one or more layers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200631704U CN201288156Y (en) | 2008-04-25 | 2008-04-25 | Novel two-stage inner-heat exchange dimethyl ether reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200631704U CN201288156Y (en) | 2008-04-25 | 2008-04-25 | Novel two-stage inner-heat exchange dimethyl ether reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201288156Y true CN201288156Y (en) | 2009-08-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2008200631704U Expired - Fee Related CN201288156Y (en) | 2008-04-25 | 2008-04-25 | Novel two-stage inner-heat exchange dimethyl ether reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108421504A (en) * | 2018-04-28 | 2018-08-21 | 南京聚拓化工科技有限公司 | Beam tube water bed type ethylene glycol hydrogenation reactor and the technique for producing ethylene glycol |
-
2008
- 2008-04-25 CN CNU2008200631704U patent/CN201288156Y/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108421504A (en) * | 2018-04-28 | 2018-08-21 | 南京聚拓化工科技有限公司 | Beam tube water bed type ethylene glycol hydrogenation reactor and the technique for producing ethylene glycol |
| CN108421504B (en) * | 2018-04-28 | 2023-08-01 | 南京聚拓化工科技有限公司 | Beam Guan Shuichuang type ethylene glycol hydrogenation reactor and process for producing ethylene glycol |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090812 Termination date: 20120425 |