CN202666813U - Axially layer by layer progressively increased chilled methanol to propylene (MTP) fixed bed reactor - Google Patents
Axially layer by layer progressively increased chilled methanol to propylene (MTP) fixed bed reactor Download PDFInfo
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- CN202666813U CN202666813U CN 201220212924 CN201220212924U CN202666813U CN 202666813 U CN202666813 U CN 202666813U CN 201220212924 CN201220212924 CN 201220212924 CN 201220212924 U CN201220212924 U CN 201220212924U CN 202666813 U CN202666813 U CN 202666813U
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Abstract
The utility model relates to an axially layer by layer progressively increased chilled methanol to propylene (MTP) fixed bed reactor. The fixed bed reactor comprises a housing (1), a hot raw gas inlet (2), a product outlet (3), cold raw gas/liquid inlets (4), cold raw material distributors (5), cold raw material nozzles (6), catalyst beds (7), inert ceramic balls (8), nitrogen nozzles (9), lateral line gas phase annular manifolds (10), lateral line liquid phase annular manifolds (11), lateral line gas phase pipes (12), lateral line liquid phase pipes (13), nitrogen distributors (14) and nitrogen inlets (15). The reactor comprises four to six beds, zeolite-based MTP catalyst is filled on the beds layer by layer in a progressively increased manner. Hot gas of raw coarse dimethyl ether or refined methanol enters the first bed from to top; cold gas and liquid enter other beds from lateral lines; and mixture of hydrocarbons, which is rich in propylene, is output from the bottom. The reactor provided by the utility model has the advantages that the magnification is easy; the back-mixing is low; the temperature is easy to control; and the mechanical loss of catalyst is low.
Description
Technical field
The utility model relates to the fixed bed reactors in a kind of preparing propylene from methanol (MTP) device, be specifically related to a kind of axially successively increment type cold shock formula fixed bed reactors that prepare propylene take thick dimethyl ether or refined methanol as raw material, belong to Coal Chemical Industry, gas chemical industry field.
Background technology
Propylene is the important petrochemical materials that is only second to ethene mainly for the production of polypropylene, acrylonitrile, expoxy propane and isopropyl alcohol etc.The in recent years fast development of acryloyl derivative has driven the rapid growth of propylene demand, and the diversification of alkene raw materials for production has become the key subjects that concern the national energy structural adjustment.The MTP(preparing propylene from methanol) technique refers to by catalytic synthesis, produce the chemical process technology of propylene take the synthetic methyl alcohol of coal-based or natural gas base as raw material.China should take full advantage of abundant methyl alcohol resource, makes great efforts exploitation MTP technique.The expert generally believes, MTP technique very likely becomes the third-largest stable source of propylene after steam cracking and catalytic cracking.
Germany LURGI (Lurgi) is the company of successful Application industrialization MTP technology in the world, and this technology becomes to contain first the mixture of dimethyl ether, unreacted methanol and steam with methanol conversion, adopt German southern chemical company
The proprietary zeolite catalyst MTPROP-1 of cooperative development further changes into mixture and is mainly propylene and contains simultaneously ethene, butylene, carbon five, C 6 olefin and high-knock rating gasoline product.Ethene, butylene, carbon five, C 6 olefin can be used as the reaction of recycle hydrocarbons sustainable participation.This reaction is the strong exothermal reaction under the zeolite based catalysts effect, and the main chemical reactions equation is:
n CH
3OH→C
nH
2n+n H
2O+Q （n=2~8）
n CH
3OCH
3(DME)→2C
nH
2n+n H
2O+Q （n=2~8）
Existing multinomial patented technology relates to this field both at home and abroad at present, such as Chinese patent CN200910195466.0, CN101080373A, CN200680008817.7 etc., but all stress on the processing technology routine method of preparing propylene from methanol, and rarely have report with regard to the engineering design of the preparing propylene from methanol fixed bed reactors of core technology itself, restricted the development of China production domesticization MTP device.Existing preparing propylene from methanol fixed bed reactors have that system's complicated operation is wayward, the high easy local temperature runaway of reaction temperature, cost of investment are high, technical backstopping foreign patent merchant's shortcoming.Therefore, satisfying under the technological requirement prerequisite, the preparing propylene from methanol fixed bed reactors that exploitation has independent intellectual property right to fill up the blank in domestic this field, have important practical significance.
Summary of the invention
In order to overcome above-mentioned shortcoming, the utility model provides a kind of axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors, and concrete technical scheme is as follows:
A kind of axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors, this reactor shell (1) top is provided with hot charge gas feed (2), housing (1) bottom is provided with product outlet (3), housing (1) inside in axial direction is provided with multi-layer catalyst bed (7), housing (1) outside between per two beds is provided with a plurality of cold unstrpped gas/liquid-inlets (4), outer gas phase annular concetrated pipe (10) and the liquid phase annular concetrated pipe (11) of arranging of reactor shell (1), distribute side line gas phase pipe (12) from annular concetrated pipe, side line liquid-phase tube (13) is connected one by one with each cold unstrpped gas/liquid-inlet (4), inject pipeline and be connected with cold feed distribution device (5) at inside reactor, the upper a plurality of cold raw material nozzles (6) of installing of cold feed distribution device (5).
Hull outside below every layer of beds arranges a nitrogen inlet (15), and the position of this import is below cold unstrpped gas/liquid-inlet, connect nitrogen distributor (14) at inside reactor from this nitrogen inlet (15), be equipped with a plurality of nitrogen nozzles (9) on the distributor or also can adopt endless tube perforate mode not join in addition nozzle.
Wherein, cold unstrpped gas/liquid-inlet (4) quantity between described per two beds is 10 ~ 20, be symmetric, the inlet direction can but be not limited to parallel injection.
Wherein, described side line gas phase pipe (12) and side line liquid-phase tube (13) can inject respectively cold unstrpped gas/liquid inlet opening (4), also can adopt the form of side line gas phase pipe (12) inner sleeve side line liquid-phase tube (13) to mix injection.
Wherein, the described liquid phase respectively form of injecting reactor is that gaseous distributer and liquid phase distributor are arranged respectively, and cold raw material nozzles (6) is used liquid-phase nozzle, and distribution of gas then evenly sprays into by the aperture of gas distributor; Cold raw material nozzles is used gas-liquid mixed phase nozzle in the injection mode of described side line gas phase pipe (12) inner sleeve side line liquid-phase tube (13).
Wherein, total number of plies of described beds is four to six layers, preferred five layers.
Wherein, the thickness of described every layer of beds (7) is 250mm ~ 700mm, and every layer of beds (7) thickness successively increases from top to bottom, and the thickness of every layer of increase is 30mm ~ 150mm.
Wherein, described beds (7) respectively is equipped with up and down inert ceramic balls (8).
Wherein, the ulking thickness of described inert ceramic balls (8) is 100mm ~ 200mm.
Wherein, described inert ceramic balls (8) is divided into 1/2 " and 1/4 " two kinds, preferred catalyst bed top is with 1/2 " pile up, the bed bottom is with 1/2 " and 1/4 " two kinds of size accumulations.
The utility model adopts above technical scheme, has advantages of as follows:
Easily amplify in the fixed bed reactors industrial production, applicability is strong, and small-scale production all is suitable for to ultra-large device.
Compare with fluid bed, fixed bed reactors Operation and Maintenance expense is low, not because the mobile wearing and tearing of equipment and pipeline and the race damage problem of catalyst of causing of catalyst occurs.It is estimated that catalyst breakage only need replenish one of the expense that causes, selecting fixed bed only is 30% ~ 50% of fluid catalyst investment.
Compare with calandria type fixed bed, the form that the utility model adopts has advantages of simple in structure, cheap, and the reactor of same size can reduce investment 40% ~ 60%.
Compare with the fixed bed of multistage multi-channel radial reaction, the form that the utility model adopts has characteristics simple in structure, that be evenly distributed, and the reactor of same size can reduce equipment investment 20% ~ 30%.
Adopt multistage cold shock formula easily to realize temperature control, keep each bed and all react at the optimal reaction temperature of catalyst, can obviously improve selective 3 ~ 5% of product.This form can in time be lowered the temperature and effectively prevented may occuring of local temperature runaway in addition, is specially adapted to strong heat release MTP reaction.
Description of drawings
Fig. 1 is the utility model preparing propylene from methanol fixed bed reactors structural representations;
Fig. 2 is the cold unstrpped gas of the utility model preparing propylene from methanol fixed bed reactors/liquid charging generalized section.
Description of reference numerals: 1-housing; The gas feed of 2-hot charge; The outlet of 3-product; Cold unstrpped gas/the liquid-inlet of 4-; The cold feed distribution device of 5-; The cold raw material nozzles of 6-; The 7-beds; The 8-inert ceramic balls; 9-nitrogen nozzle; 10-side line gas phase annular concetrated pipe; 11-side line liquid phase annular concetrated pipe; 12-side line gas phase pipe; 13-side line liquid-phase tube; 14-nitrogen distributor; The 15-nitrogen inlet.
The specific embodiment
Fig. 1 is the utility model preparing propylene from methanol fixed bed reactors structural representations, and wherein, 1 is housing, is top and the bottom and is the cylinder of circle end socket; 2 is the hot charge gas feed; 3 are the product outlet; 4 is cold unstrpped gas/liquid-inlet; 5 is cold feed distribution device; 6 is liquid-phase nozzle; 7 is beds; 8 is inert ceramic balls; 9 is the nitrogen cooling jet; 14-nitrogen distributor; The 15-nitrogen inlet.
Fig. 2 is the cold unstrpped gas of the utility model preparing propylene from methanol fixed bed reactors/liquid charging generalized section, and wherein, 4 is cold unstrpped gas/liquid-inlet, and 5 is cold feed distribution device; 10 is side line gas phase annular concetrated pipe; 11 is side line liquid phase annular concetrated pipe; 12 is side line gas phase pipe; 13 is the side line liquid-phase tube.
The thick dimethyl ether of raw material (DME) or refined methanol enter reactor from reactor head and side line respectively, wherein hot phase raw material and recycle hydrocarbons enter the first bed from top hot charge gas feed 2, cold air phase raw material and liquid phase feed successively (except ground floor) enter remaining bed by the cold unstrpped gas/liquid-inlet 4 of sidepiece, reactant need not cooling after the reaction of last bed, (product of C2 ~ C8) exports 3 extraction from the reactor bottom product and enters the later separation unit to be rich in the hydrocarbon mixture of propylene.
The raw material of reactor can be thick dimethyl ether or refined methanol.Thick dimethyl ether derives from the upstream dimethyl ether reactor by the product of refined methanol catalytic synthesising dimethyl ether, and its mole consists of dimethyl ether 30% ~ 40%, methyl alcohol 10% ~ 30%, and water 30% ~ 50% contains a small amount of carbon three, carbon four hydro carbons.Preferred mole consists of dimethyl ether 40%, methyl alcohol 20%, water 40%.Purity derives from the product of methanol synthesizer greater than the refined methanol of 95%wt, refined methanol directly enters this preparing propylene from methanol fixed bed reactors catalytic reaction, is rich in the hydrocarbon mixture of propylene via reaction generation dimethyl ether intermediate product and then generation.
The top fed mouth is the gas phase mixture of the recycle hydrocarbons returned of thick dimethyl ether or refined methanol and later separation unit, and temperature range is controlled at 450 ℃ ~ 480 ℃, preferred 470 ℃.Cold unstrpped gas/the liquid inlet opening 4 of sidepiece is respectively gas phase and the liquid phase of cold thick dimethyl ether or refined methanol and injects respectively, and the gas phase temperature scope control is at 180 ℃ ~ 280 ℃, and preferred 190 ~ 210 ℃, gas phase temperature successively can be identical, also can form gradient; The liquidus temperature scope control is at 50 ℃ ~ 70 ℃, preferred 65 ℃.
Because the preparing propylene from methanol reaction is strong exothermal reaction, for effective, the safe large calorimetric that reaction produces of withdrawing, limit the rapid rising of adiabatic bed temperature, this reactor adopts successively cold shock formula, cold unstrpped gas and cold raw material liq are entered reactor from the lower side import 4 of each beds 7, the reacted high-temperature product of each bed enters lower one deck catalyst bed reaction after importing immediately fresh cold raw material dilution cooling again, all reacts at the optimal reaction temperature that catalyst is recommended to guarantee each bed.
Because maximizing, unit scale cause reactor diameter bigger than normal, avoid the dead angle to produce in order to guarantee that the cold raw material injecting reactor of sidepiece evenly distributes, take away timely and effectively a large amount of reaction heat, needing to consider to arrange cold feed distribution device 5 helps to distribute, and distributor can effectively reduce by two distances between the bed, thereby reduces the height of whole reactor.The implementation way is opened a plurality of cold unstrpped gas/liquid inlet openings 4 for sidepiece between each bed of employing, the charging aperture direction can but be not limited to parallel injection, be arranged symmetrically with, charging aperture quantity is 10 ~ 20, and the spray angle of quantity visual response device size and cold raw material nozzles 6 determines.Each charging aperture all has cold raw material (thick dimethyl ether or refined methanol) gas phase and liquid phase to inject, therefore the reactor shell external demand arranges gas phase annular concetrated pipe 10 and liquid phase annular concetrated pipe 11, from annular concetrated pipe distribute side line gas phase pipe 12, side line liquid-phase tube 13 is connected one by one with each cold material inlet 4.Side line gas phase pipe 12 and side line liquid-phase tube 13 can be distinguished injecting feeding mouth 4, also can adopt the form of side line gas phase pipe 12 inner sleeve side line liquid-phase tubes 13 to mix injection.Injecting pipeline is connected with cold feed distribution device 5 at inside reactor, the parallel inside reactor that is evenly arranged in of distributor, the cold raw material nozzles 6 of the terminal installation of distributor, form for liquid phase difference injecting reactor, gaseous distributer and liquid phase distributor are arranged respectively, cold raw material nozzles 6 selects liquid-phase nozzle to help uniform liquid to distribute, and distribution of gas then evenly sprays into by the aperture of gas distributor; For the injection mode of side line gas phase pipe 12 inner sleeve side line liquid-phase tubes 13, cold raw material nozzles need be selected gas-liquid mixed phase nozzle.
Described reactor catalyst bed 7 is four to six layers, preferred five layers.Bed is filled zeolite based ZSM-5 or modified ZSM-5 MTP catalyst, requirement according to 10 ~ 15 ℃ of each beds temperature rises of control, along with the reaction mass of sneaking into of cold shock material successively increases, the beds loadings is different, filling thickness successively increases from top to bottom, thickness is 250mm ~ 700mm, and the thickness of every layer of increase is 30mm ~ 150mm.The weight (hourly) space velocity (WHSV) of reactor is 0.5 ~ 1.5 thick dimethyl ether (or refined methanol)/(kg catalyst .hr), is preferably 0.7 ~ 1.0 thick dimethyl ether (or refined methanol)/(kg catalyst .hr).
Every bed all has up and down inert ceramic balls 8 to lay, and as support and the cladding material of catalyst in reactor, available buffer enters in the reactor liquids and gases to the impact of catalyst, guard catalyst, and improve the distribution of liquids and gases in the reactor.Inert ceramic balls is divided into 1/2 " and 1/4 " two kinds, recommend beds top with 1/2 " pile up, the bed bottom is with 1/2 " and 1/4 " two kinds of size accumulations, the piling height of two kinds of sizes can be identical or different, and piling height is 100mm ~ 200mm.
In emergency circumstances cooling scheme below described reactor adopts: adopt the method that sprays into nitrogen to prevent the reactor temperature runaway, hull outside below every layer of beds arranges a nitrogen inlet 15, and the position of this import is below cold unstrpped gas/liquid-inlet, connect nitrogen distributor 14 at inside reactor from this nitrogen inlet 15, be equipped with a plurality of nitrogen nozzles 9 on the distributor.Nozzle spray direction and reaction mass are rightabout, and reverse contact guarantees that cooling rapidly.The quantity of nitrogen nozzle 9 and angle visual response device size determine, perhaps also can adopt endless tube perforate mode not join in addition nozzle.
According to the requirement of catalyst regeneration operation, for assurance device moves continuously, need a reactor for subsequent use for switching in the actual production.According to the needs of unit scale output, reactor can arrange many parallel operations, for the requirement that guarantees that the catalyst time of staying and product performance reach unanimity, and the reactor specification that recommend adoption is identical.
Embodiment 1
Take a MTP device of producing 500000 ton/years of propylene per year as example, three reactors are set, two of normal operatings, a regeneration is for subsequent use, and three reactor specifications are identical.This reactor is thick dimethyl ether charging operating mode, and its mole consists of dimethyl ether 40%, methyl alcohol 20%, water 40%.This reactor working pressure range is 0.03MPaG ~ 0.13MPaG, and the range of reaction temperature of each bed is 470 ℃ ~ 480 ℃, and the temperature rise control range by each bed catalyst is 10 ℃.
Reactor is established five layers of beds altogether, filling modified ZSM-5 MTP catalyst, catalyst calculates according to the weight (hourly) space velocity (WHSV) of 0.7 thick dimethyl ether/(kg catalyst .hr), inert ceramic balls top lays 1/2 "; the bottom lays 1/4 " and 1/2 " respectively half, the bed height that successively increases progressively and the laying depth of inert ball see Table 1:
The thickness of table 1 beds and inert ball (thick dimethyl ether charging)
470 ℃ ~ 480 ℃ thick gas of dimethyl ether and from the systemic circulation hydrocarbon mixture (mole forms: methane 4%, C 2 hydrocarbon 22%, carbon three hydrocarbon 0.5%, carbon four hydrocarbon 29%, carbon five hydrocarbon 26%, carbon six hydrocarbon 17%, other are impurity) enter reactor stream after the ground floor beds from top hot charge gas feed 2, add fresh 190 ℃ of cold thick gas of dimethyl ether and 65 ℃ of thick dimethyl ether liquid from the cold unstrpped gas/liquid-inlet 4 of sidepiece, the weight ratio of each bed total feed of top fed amount and side line is 2:1, the inlet amount of the thick dimethyl ether of liquid phase is 10% (wt) of side direction charging total amount, and the reactor outlet temperature is controlled at 480 ℃ ~ 490 ℃.
This reactor diameter is at 10000mm, every bed arranges 12 cold unstrpped gas/liquid-inlets, be arranged symmetrically with parallel injection, one side is 6, side line gas phase pipe 12 and side line liquid-phase tube 13 injecting reactors that cold unstrpped gas and liquid are drawn from gas phase annular concetrated pipe 10 and liquid phase annular concetrated pipe 11 respectively, the form that the cold feed distribution device 5 of inside reactor distributes respectively for gas, liquid, the cold raw material nozzles quantity that is used for liquid distribution is 60 (single-layer catalyst beds), and Gas distribution evenly sprays into by the aperture (Φ 5mm) of distributor.
Take a MTP device of producing 600000 ton/years of propylene per year as example, three reactors are set, two of normal operatings, a regeneration is for subsequent use, and three reactor specifications are identical.This reactor is refined methanol (methanol purity is greater than 95%) charging operating mode.This reactor working pressure range is 0.03MPaG ~ 0.13MPaG, and the range of reaction temperature of each bed is 460 ℃ ~ 470 ℃, and the temperature rise control range by each bed catalyst is 12 ℃.
Reactor is established five layers of beds altogether, filling modified ZSM-5 MTP catalyst, catalyst calculates according to the weight (hourly) space velocity (WHSV) of 0.9 refined methanol/(kg catalyst .hr), inert ceramic balls top lays 1/2 "; the bottom lays 1/4 " and 1/2 " respectively half, the thickness of bed layer that successively increases progressively and the laying depth of inert ball see Table 2:
The thickness of table 2 beds and inert ball (refined methanol charging operating mode)
460 ℃ ~ 470 ℃ refined methanol gas and from the systemic circulation hydrocarbon mixture (mole forms: methane 4%, C 2 hydrocarbon 22%, carbon three hydrocarbon 0.5%, carbon four hydrocarbon 29%, carbon five hydrocarbon 26%, carbon six hydrocarbon 17%, other are impurity) enter reactor stream after the ground floor beds from top hot charge gas feed 2, add 180 ℃ of cold refined methanol gases and 65 ℃ of refined methanol liquid from the cold unstrpped gas/liquid-inlet 4 of sidepiece, the weight ratio of each bed total feed of top fed amount and side line is 2:1, the inlet amount of the thick dimethyl ether of liquid phase is 10% (wt) of side direction charging total amount, and the reactor outlet temperature is controlled at 472 ℃ ~ 482 ℃.
This reactor diameter is at 11000mm, every bed arranges 18 cold unstrpped gas/liquid-inlets, be arranged symmetrically with parallel injection, one side is 9, side line gas phase pipe 12 and side line liquid-phase tube 13 injecting reactors that cold unstrpped gas and liquid are drawn from gas phase annular concetrated pipe 10 and liquid phase annular concetrated pipe 11 respectively, the form that the cold feed distribution device 5 of inside reactor is gas, liquid sleeve pipe, cold raw material nozzles 6 adopts the liquid phase mixing nozzle, and quantity is 66 (single-layer catalyst beds).
Embodiment 3 nitrogen temperature control schemes
A nitrogen inlet 15 is set below every layer of beds, and the position of this entrance is below cold unstrpped gas/liquid-inlet 4, connect nitrogen distributor 14 at inside reactor from this nitrogen inlet, distributor is managed layout ringwise, be equipped with a plurality of nitrogen nozzles 9 on the distributor, injection direction guarantees to lower the temperature with reverse the contact rapidly of reacting gas from bottom to top, and nozzle quantity is 20, and nozzle spray angle is 30 ° ~ 60 °.Also can adopt endless tube perforate (Φ 5mm) mode not join in addition nozzle.Nitrogen recommend adoption high pressure nitrogen (5.4 ~ 5.9MPaG, environment temperature), when reactor point for measuring temperature temperature is increased to alarming value (usually being located at higher 30 ~ 40 ℃ than well-defined reaction temp), automatically open the interlocking valve gate open and enter high pressure nitrogen, this moment, the nitrogen cooling tube of each bed all sprayed the nitrogen cooling, when temperature is down to well-defined reaction temp, chain valve autoshutdown.In order to ensure in time spraying into of high pressure nitrogen, each reactor is equipped with a high pressure nitrogen surge tank, and this tank is arranged on around the reactor.
Above-described embodiment is described preferred embodiment of the present utility model; be not that scope of the present utility model is limited; under the prerequisite that does not break away from the utility model design spirit; various distortion and improvement that those of ordinary skills make the technical solution of the utility model all should fall in the definite protection domain of the utility model claims.
Claims (11)
1. axial successively increment type cold shock formula preparing propylene from methanol fixed bed reactors, it is characterized in that, this reactor shell (1) top is provided with hot charge gas feed (2), housing (1) bottom is provided with product outlet (3), housing (1) inside in axial direction is provided with multi-layer catalyst bed (7), housing (1) outside between per two beds is provided with a plurality of cold unstrpped gas/liquid-inlets (4), outer gas phase annular concetrated pipe (10) and the liquid phase annular concetrated pipe (11) of arranging of reactor shell (1), distribute side line gas phase pipe (12) from annular concetrated pipe, side line liquid-phase tube (13) is connected one by one with each cold unstrpped gas/liquid-inlet (4), inject pipeline and be connected with cold feed distribution device (5) at inside reactor, the upper a plurality of cold raw material nozzles (6) of installing of cold feed distribution device (5).
2. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 1, it is characterized in that, hull outside below every layer of beds arranges a nitrogen inlet (15), and the position of this import is below cold unstrpped gas/liquid-inlet, connect nitrogen distributor (14) at inside reactor from this nitrogen inlet (15), be equipped with a plurality of nitrogen nozzles (9) on the distributor or also can adopt endless tube perforate mode not join in addition nozzle.
3. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 1, it is characterized in that, cold unstrpped gas/liquid-inlet (4) quantity between described per two beds is 10 ~ 20, be symmetric, the inlet direction can but be not limited to parallel injection.
4. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 1, it is characterized in that, described side line gas phase pipe (12) and side line liquid-phase tube (13) can inject respectively cold unstrpped gas/liquid inlet opening (4), also can adopt the form of side line gas phase pipe (12) inner sleeve side line liquid-phase tube (13) to mix injection.
5. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 4, it is characterized in that, the described liquid phase respectively form of injecting reactor is that gaseous distributer and liquid phase distributor are arranged respectively, cold raw material nozzles (6) is used liquid-phase nozzle, and distribution of gas then evenly sprays into by the aperture of gas distributor; Cold raw material nozzles is used gas-liquid mixed phase nozzle in the injection mode of described side line gas phase pipe (12) inner sleeve side line liquid-phase tube (13).
6. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 1 is characterized in that, total number of plies of described beds is four to six layers.
7. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 6 is characterized in that, total number of plies of described beds is five layers.
8. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 1, it is characterized in that, the thickness of described every layer of beds (7) is 250mm ~ 700mm, every layer of beds (7) thickness successively increases from top to bottom, and the thickness of every layer of increase is 30mm ~ 150mm.
9. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 1 is characterized in that, described beds (7) inert ceramic balls (8) respectively is housed up and down.
10. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 9 is characterized in that, the ulking thickness of described inert ceramic balls (8) is 100mm ~ 200mm.
11. axially successively increment type cold shock formula preparing propylene from methanol fixed bed reactors according to claim 9, it is characterized in that, described inert ceramic balls (8) is divided into 1/2 " and 1/4 " two kinds, preferred catalyst bed top is with 1/2 " pile up, the bed bottom is with 1/2 " and 1/4 " two kinds of size accumulations.
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| CN 201220212924 CN202666813U (en) | 2012-05-07 | 2012-05-07 | Axially layer by layer progressively increased chilled methanol to propylene (MTP) fixed bed reactor |
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| CN 201220212924 CN202666813U (en) | 2012-05-07 | 2012-05-07 | Axially layer by layer progressively increased chilled methanol to propylene (MTP) fixed bed reactor |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102671580A (en) * | 2012-05-07 | 2012-09-19 | 中国寰球工程公司 | Axial bed-increased type quenching methanol-to-propylene (MTP) fixed bed reactor |
| CN104109072A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Methanol-to-olefin reaction apparatus and application thereof |
| CN104437267A (en) * | 2013-09-24 | 2015-03-25 | 中国石油化工股份有限公司 | Device for preparing olefin with oxygen compounds and application of device for preparing olefin with oxygen compounds |
| CN105771810A (en) * | 2014-12-25 | 2016-07-20 | 中国石油天然气股份有限公司 | Reactor for alkylation of benzene and methyl alcohol and feeding method |
| WO2020182138A1 (en) * | 2019-03-11 | 2020-09-17 | 北京诺维新材科技有限公司 | Method for improving reaction yield |
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2012
- 2012-05-07 CN CN 201220212924 patent/CN202666813U/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102671580A (en) * | 2012-05-07 | 2012-09-19 | 中国寰球工程公司 | Axial bed-increased type quenching methanol-to-propylene (MTP) fixed bed reactor |
| CN104109072A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Methanol-to-olefin reaction apparatus and application thereof |
| CN104109072B (en) * | 2013-04-16 | 2017-03-15 | 中国石油化工股份有限公司 | The reaction unit of methanol-to-olefins and its application |
| CN104437267A (en) * | 2013-09-24 | 2015-03-25 | 中国石油化工股份有限公司 | Device for preparing olefin with oxygen compounds and application of device for preparing olefin with oxygen compounds |
| CN104437267B (en) * | 2013-09-24 | 2017-05-17 | 中国石油化工股份有限公司 | Device for preparing olefin with oxygen compounds and application of device for preparing olefin with oxygen compounds |
| CN105771810A (en) * | 2014-12-25 | 2016-07-20 | 中国石油天然气股份有限公司 | Reactor for alkylation of benzene and methyl alcohol and feeding method |
| WO2020182138A1 (en) * | 2019-03-11 | 2020-09-17 | 北京诺维新材科技有限公司 | Method for improving reaction yield |
| US11338262B2 (en) | 2019-03-11 | 2022-05-24 | Novashin Co., Ltd. | Method for improving reaction yield |
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