CN203303923U - Alkylation reactor - Google Patents
Alkylation reactor Download PDFInfo
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- CN203303923U CN203303923U CN2013203334965U CN201320333496U CN203303923U CN 203303923 U CN203303923 U CN 203303923U CN 2013203334965 U CN2013203334965 U CN 2013203334965U CN 201320333496 U CN201320333496 U CN 201320333496U CN 203303923 U CN203303923 U CN 203303923U
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- catalytic bed
- communicated
- catalyst
- central tube
- inner core
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Abstract
The utility model discloses an alkylation reactor. In order to solve the problems that the mass content of CO and CO2 in an ammonia material gas is greater than 10PPM, so that oxidation poisoning on an ammonia synthesis catalyst is easily generated, the alkylation reactor comprises an outer barrel and an inner barrel, wherein an annular space is formed between the outer barrel and the inner barrel; an air inlet a is formed at the upper part of the outer barrel; a central pipe is arranged inside the inner barrel; a plurality stages of catalyst beds are arranged between the inner barrel and the central pipe; two stages of adjacent catalyst beds are communicated through a communicating pipe; air hole plates are arranged at the upper side and the lower side of each stage of catalyst bed; an air outlet b is arranged at the bottom of the outer barrel; the air outlet b is connected with a steam heater through a heat exchanger; the outlet of the steam heater is communicated with the lower end of the central pipe; an air outlet c is arranged at the bottom of the inner barrel; the air outlet c is connected with next procedure equipment through the heat exchanger. By adopting the alkylation reactor, mixed ammonia material gas of 0.05-3% by mass of CO and CO2 can be alkylated until the mass content of the CO and CO2 is smaller than 10PPM.
Description
Technical field
The utility model relates to the alkylation reaction apparatus field, is specially a kind of alkylation reaction device.
Background technology
A small amount of CO, CO
2In the ammonia unstripped gas, contain a small amount of CO, CO
2(the quality percentage composition is 0.05%～0.2%), a small amount of CO, CO
2To ammonia synthesis catalyst, there is oxidation poisoning, must remove to 10PPM.This process is called refining.A kind of process for purification is arranged by CO, CO
2Be converted into hydrocarbonize compound (hydrocarbonylation), chemical equation:
CO+2nH
2→(CH
2)
n+H
2O+Q
CO+2H
2→CH
3OH?+Q
CO+3H
2→CH
4+H
20+Q
CO+H
2O→CO
2+H
2+Q
Above-mentioned reaction is heat release, and reacts in the tower of certain catalyst is housed.If thermal insulation is reacted, to generate CH
4For example, 72 ℃ of every reaction 1%CO temperature rises, every reaction 1%CO
259 ℃ of temperature rises.
Owing in the ammonia unstripped gas, containing quality percentage composition approximately 0.15% CO and about 0.05% CO
2, temperature rise=(0.15 * 70)+(0.05 * 59)=13.45 ℃; Because when reaction, catalytic tower had heat loss, and the reaction heat of emitting is not enough offsets heat loss, thereby temperature do not rise counter falling, and namely requires outer heat supply, steadily carries out at a certain temperature to maintain reaction.
The utility model content
In order to overcome CO and CO in existing ammonia unstripped gas
2Mass content is greater than 10PPM, easily ammonia synthesis catalyst is produced to the poisoning deficiency of oxidation, the utility model aims to provide a kind of alkylation reaction device, and this alkylation reaction device can be that 0.05% ~ 3% CO+CO2 mixing ammonia unstripped gas hydrocarbonylation is to CO and CO by the quality percentage composition
2Mass content be less than 10PPM.
To achieve these goals, the technical scheme that adopts of the utility model is:
A kind of alkylation reaction device, comprise urceolus and inner core, is provided with annular space between this urceolus and inner core; Described urceolus top is provided with air inlet a; Its design feature is, in described inner core, be provided with central tube, between this inner core and central tube, be provided with top-down multistage catalytic bed, between adjacent two-stage catalytic bed by being communicated with communicating pipe, and upper level catalytic bed is communicated with described central tube upper end, and the side up and down of every grade of catalytic bed is provided with the air passing hole plate; Described urceolus bottom is provided with gas outlet b, and this gas outlet b is connected with steam heater by heat exchanger, and the outlet of described steam heater is communicated with described central tube lower end; Described inner core bottom is provided with the gas outlet c be communicated with next stage catalytic bed, and this gas outlet c is connected with subsequent processing equipment by heat exchanger.
The aperture of the air passing hole plate of catalytic bed described in the utility model is less than the grain diameter of catalyst, guarantee gas by and catalyst does not leak down.
Be below the technical scheme of further improvement of the utility model:
In order between described adjacent two-stage catalytic bed, to be provided with the gas collection cavity, gas continues alkylation reaction toward the next stage catalytic bed again through the gas collection cavity after by the upper level catalytic bed, reacting.
In order to be convenient for changing catalyst, described urceolus top is provided with charging pipe, and this charging pipe is connected with the catalyst basin by valve; Described urceolus bottom is provided with discharge duct; While needing the filling reduction catalyst, close each valve with the reactor connecting pipe, the closed discharging pipe, in reactor, be filled with nitrogen, keep malleation, by the reduction catalyst bucket, connecting hose is connected with charging pipe, opens catalyst barreled bottom valve, catalyst automatically flows into internals and fills up.
Between described next stage catalytic bed and inner core bottom, be provided with a plurality of porcelain balls, reacted gas, by the gap between the porcelain ball, then enters in heat exchanger by gas outlet c.
In described central tube, be provided with electric furnace, when raw catelyst need to heat up heated air, or steam heater uses while breaking down.
According to embodiment of the present utility model, described catalytic bed comprises two-stage, is respectively catalytic bed and lower catalytic bed; Described upper catalytic bed is communicated with described central tube top, and described lower catalytic bed is communicated with gas outlet c.
Alkylation reaction process using of the present utility model alkylation reaction device as above, its processing step comprises:
1) by the quality percentage composition, be that 0.05% ~ 3% CO enters the annular space between inside and outside cylinder with CO2 mixing ammonia unstripped gas through air inlet a, then downwards after gas outlet b enters in heat exchanger and is heated to 185 ℃～195 ℃, then send in steam heater and be heated to 215 ℃～225 ℃;
2) gas after steam heater heating enters in central tube, in the central tube top enters multistage catalytic bed, carries out the quality percentage composition<10PPM of alkylation reaction to CO gas and CO2;
3) gas after alkylation reaction enters in heat exchanger and is cooled to 70 ℃～100 ℃ by gas outlet c, then by after water-cooled cooling, sending into subsequent processing.
In step 1), 260 ℃～280 ℃ superheated steams of steam employing in described steam heater or the saturated vapor of 240 ℃～250 ℃.
Generally speaking, the temperature after described water-cooled cooling is 30 ℃ ~ 50 ℃.
In the utility model, in described catalytic bed, reduction catalyst is housed; During the filling reduction catalyst, close with the reactor connecting pipe on each valve, and the discharge duct of sealing urceolus bottom, in reactor, be filled with nitrogen again, keep malleation, then the catalyst basin is connected with the charging pipe on urceolus top by connecting hose, opens the valve of emitting of catalyst basin, reduction catalyst automatically flows in catalytic beds at different levels and fills up.Certainly, can also load the pre-reduction type catalyst in catalytic bed of the present utility model, after filling pre-reduction type or reduction catalyst, temperature only reaches 200 ℃ can drop into normal production, and furnace power reduces 1/3.
By said structure, the utility model relates to a small amount of CO, CO
2Hydrocarbonylation or methanation reaction and flow process, be applied to contain a small amount of CO, CO
2Purified synthesis gas, be refined to PPM level field.
Compared with prior art, the beneficial effects of the utility model are:
1, simple in structure, existing similar techniques is that cold and hot gas-heat exchanger is arranged at the bottom of inner core, or in catalytic bed, cooler tube bundle is arranged, complex structure/long flow path.The utility model does not have bottom that cold and hot gas-heat exchanger and cooler tube bundle are arranged.
2, the loading and unloading catalyst is easy, once automatically completes during filling, and the time is short; While unloading catalyst, as long as open the discharge duct blind plate, catalyst unloads automatically, only completes in several hours.
3, in inner core without heat exchanger, cooler tube bundle, the high-pressure space utilization rate is up to 75%, Catalyst packing is many, refining ability is large;
4,, without special high pressure resistant, the anti-hydrogen Steel material of high temperature, only need common CrMo steel, low cost.
5, energy-conservation: existing similar techniques is the unlatching electric furnace that is in operation, with the maintaining heat balance.Middle pressure saturated vapor or turbine back pressure superheated steam recycling that the utility model utilizes waste heat recovery to produce, heating unreacting gas to 215 ℃～225 ℃.
6, shorten the production time that goes into operation, only shortened to and need 8～10 hours by seven days that have technique now, save the driving expense of large number.
Below in conjunction with drawings and Examples, the utility model is further elaborated.
The accompanying drawing explanation
Fig. 1 is the structure principle chart of an embodiment of the utility model.
In the drawings
The 1-urceolus; The 2-inner core; 3-upper strata catalyst; The 4-up-hole plate; 5-catalyst communicating pipe; 6-gas collection cavity; The 7-central tube; Catalyst layer under 8-; The 9-electric furnace; The 10-orifice plate; 11-porcelain ball; The 12-discharge duct; Filler in the 13-threeway; Filler under the 14-threeway; Threeway at the bottom of the 15-tower; The 16-heat exchanger; The 17-steam heater; The 19-charging pipe; The 20-connecting hose; The 21-valve; 22-catalyst basin.
The specific embodiment
A kind of alkylation reaction device, as shown in Figure 1, this reactor by pressurized heavy wall urceolus 1, formed by warm inner core 2, upper catalytic bed 3, up-hole plate 4, communicating pipe 5, gas collection cavity 6, central tube 7, lower catalytic bed 8, electric furnace 9, orifice plate 10, porcelain ball 11, discharge duct 12.Upper and lower two groups of threeway fillers 13,14 are arranged at the bottom of tower, separate reaction gas and unreacting gas.Catalyst by upper and lower orifice plate 4,10 supportings, is drilled with many apertures respectively on plate, the above is covered with one to two layer of silk screen, and reaction gas is negotiable to lower floor, and catalyst can not leak down.
To contain the quality percentage composition and be 0.05% ~ 3% CO+CO2 mixing ammonia unstripped gas is entered by the reactor top a mouth of pipe, from the annular space between inner/outer tube, go out reactor to the reactor lower part b mouth of pipe from top to bottom, after entering heat exchanger 16 and being heated to 185 ℃～195 ℃, enter again overheating steam heater 17, by 260 ℃～280 ℃ superheated steams (also can utilize the saturated vapor of 240 ℃～250 ℃), be heated to 215 ℃～225 ℃, from the d mouth of pipe of threeway 13 at the bottom of tower, enter reactor inner central tube 7, from bottom to top arrive inner core 2 upper spaces, then be folded to and enter catalytic bed 3 downwards, axially by upper bed layer, react, reacting gas combines in gas collection cavity 6, flow downstream into orifice plate 10, aperture on its plate body respectively, enter in lower catalytic bed 8, axially by after lower catalytic bed 8 reactions, CO+CO2<10PPM in gas, reacting gas combines in lower gas collection cavity 6, flow downstream into the inner core lower space, again down through tee-joint sleeve to gas outlet c, enter heat exchanger 16 and be cooled to 70 ℃～100 ℃, approximately 40 ℃ of the cold coolings of intaking, send subsequent processing.
Central tube arranges electric furnace 9, for raw catelyst intensification heated air use, or uses when overheating steam heater 17 breaks down, need not while normally producing.
Catalyst of the present utility model is pre-reduction type or reduced form, because reduction catalyst can not be cruelly in air, filling is during reduction catalyst, closes each valve with the reactor connecting pipe, the closed discharging pipe, in reactor, be filled with nitrogen, keep malleation, by reduction catalyst bucket 22, connecting hose 20 is connected with charging pipe 19, open catalyst barreled bottom valve 21, catalyst automatically flows into internals and fills up.
With the reduction catalyst bucket 22 of valve 21 and 20 need of connecting hose, just winch to reactor position as shown in Figure 1 toward annotating in reactor while filling catalyst.
Catalyst of the present utility model is pre-reduction type or reduced form, hydrocarbonylation catalyst for example, and wherein a kind of Main Ingredients and Appearance is Fe
2O
3, oxygen wherein has been Fe by the hydrogen reduction reaction formula
2O
3+ H
2→ Fe+H
2O(vapour), the iron in formula is the solid particle that countless micropores are arranged, and isolated air is stored in basin, and tank bottom is provided with valve and charging pipe.
Because non-reduced hydrocarbonylation catalyst temperature when reduction need to reach 480 ℃～490 ℃, in central tube, furnace power is large, and the central tube diameter is large, takes up room many, has dwindled loaded catalyst; Reduction temperature reaches 480 ℃～490 ℃, and the bottom threeway of high temperature reduction gas process will be selected the anti-hydrogen precious materials of high temperature.And after the utility model filling pre-reduction type or reduction catalyst, temperature only reaches 200 ℃ can drop into normal production, furnace power reduces 1 ∕ 3, and the bottom threeway only selects common CrMo steel to get final product.
The content that above-described embodiment is illustrated should be understood to these embodiment only be used to being illustrated more clearly in the utility model, and be not used in the restriction scope of the present utility model, after having read the utility model, those skilled in the art all fall within the application's claims limited range to the modification of the various equivalent form of values of the present utility model.
Claims (6)
1. an alkylation reaction device, comprise urceolus (1) and inner core (2), is provided with annular space between this urceolus (1) and inner core (2); Described urceolus (1) top is provided with air inlet a; It is characterized in that, in described inner core (2), be provided with central tube (7), between this inner core (2) and central tube (7), be provided with top-down multistage catalytic bed (3,8), adjacent two-stage catalytic bed (3,8) between, be communicated with by communicating pipe (5), and upper level catalytic bed (3) is communicated with described central tube (7) upper end, the side up and down of every grade of catalytic bed is provided with the air passing hole plate; Described urceolus (1) bottom is provided with gas outlet b, and this gas outlet b is connected with steam heater (17) by heat exchanger (16), and the outlet of described steam heater (17) is communicated with described central tube (7) lower end; Described inner core (2) bottom is provided with the gas outlet c is communicated with next stage catalytic bed (8), and this gas outlet c passes through heat exchanger (16) and is connected with subsequent processing equipment.
2. alkylation reaction device according to claim 1, is characterized in that, between described adjacent two-stage catalytic bed (3,8), is provided with gas collection cavity (6).
3. alkylation reaction device according to claim 1, is characterized in that, in described central tube (7), is provided with electric furnace (9).
4. alkylation reaction device according to claim 1, is characterized in that, described urceolus (1) top is provided with charging pipe (19), and this charging pipe (19) is connected with catalyst basin (22) by valve (21); Described urceolus (1) bottom is provided with discharge duct (12).
5. alkylation reaction device according to claim 1, is characterized in that, is provided with a plurality of porcelain balls (11) between described next stage catalytic bed (8) and inner core (2) bottom.
6. according to the described alkylation reaction device of one of claim 1 ~ 5, it is characterized in that, described catalytic bed (3,8) comprises two-stage, is respectively catalytic bed (3) and lower catalytic bed (8); Described upper catalytic bed (3) is communicated with described central tube (7) top, and described lower catalytic bed (8) is communicated with gas outlet c.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203334965U CN203303923U (en) | 2013-06-09 | 2013-06-09 | Alkylation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203334965U CN203303923U (en) | 2013-06-09 | 2013-06-09 | Alkylation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203303923U true CN203303923U (en) | 2013-11-27 |
Family
ID=49610159
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013203334965U Withdrawn - After Issue CN203303923U (en) | 2013-06-09 | 2013-06-09 | Alkylation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203303923U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103272534A (en) * | 2013-06-09 | 2013-09-04 | 湖南安淳高新技术有限公司 | Alkylation reactor and alkylation technology |
| CN107281993A (en) * | 2016-03-30 | 2017-10-24 | 中国科学院上海应用物理研究所 | Reactor and reaction system and operation method including it |
-
2013
- 2013-06-09 CN CN2013203334965U patent/CN203303923U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103272534A (en) * | 2013-06-09 | 2013-09-04 | 湖南安淳高新技术有限公司 | Alkylation reactor and alkylation technology |
| CN107281993A (en) * | 2016-03-30 | 2017-10-24 | 中国科学院上海应用物理研究所 | Reactor and reaction system and operation method including it |
| CN107281993B (en) * | 2016-03-30 | 2021-03-26 | 中国科学院上海应用物理研究所 | Reactor, reaction system comprising same and operation method |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20131127 Effective date of abandoning: 20150225 |
|
| RGAV | Abandon patent right to avoid regrant |