CN202447060U - Multi-tube oxidation reactor - Google Patents
Multi-tube oxidation reactor Download PDFInfo
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- CN202447060U CN202447060U CN2011205685280U CN201120568528U CN202447060U CN 202447060 U CN202447060 U CN 202447060U CN 2011205685280 U CN2011205685280 U CN 2011205685280U CN 201120568528 U CN201120568528 U CN 201120568528U CN 202447060 U CN202447060 U CN 202447060U
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Abstract
The utility model discloses a multi-tube oxidation reactor which comprises a reactor cylinder body and is characterized in that the reactor cylinder body internally provides an upper part, a middle part and a lower part, wherein the lower part is a reaction gas distribution region, the middle part is a reaction region, the upper part is a product gas heat exchange region, a plurality of sleeves parallel with a longitudinal axis of the reactor cylinder body are arranged in the reactor cylinder body and below the product gas heat exchange region, the sleeves are arranged on the cross section of the reactor cylinder body, the reaction gas distributing region is used for respectively averagely distributing two reaction gases to all sleeves, each sleeve comprises an inner tube and an outer tube, the inner tube is used for introducing the first reaction gas, and a ring gap between the inner tube and the outer tube is used for introducing the second reaction gas. The multi-tube oxidation reactor can effectively solve the problems of overlarge local temperature rise and influenced reaction selectivity caused by oxidization reaction heat release concentration.
Description
Technical field
The utility model relates to gas phase oxidation reactor, relates in particular to the reactor that the exothermic heat of reaction amount is big, product at high temperature decomposes and do not adopt the gas phase oxidation of catalyst easily.
Background technology
Gas phase oxidation is an important and commonly used synthetic reaction, and the oxidation reaction of modal ethene, acetylene can be emitted a large amount of reaction heat usually.According to different reaction characteristicses, produced different structure of reactor forms, and various reaction heat removes mode.For the initiation that is applicable to the oxidation reaction that does not need catalyst with continue, obtain product efficiently and need preferred suitable reactor.
The two-in-one graphite hydrogen chloride synthetic furnace of Chinese patent CN200320120265.2 combined type; The reactor that chlorine and hydrogen carry out oxidation reaction has been described; Reacting gas is located the oxidation reaction that hybrid concurrency is given birth to strong heat release at " lamp holder ", and lamp cap device adopts the multi-barrel formula, and chlorine, hydrogen are mixed; Burning is thorough, and product hydrogen chloride is at high temperature more stable.This structure of reactor is simple, and efficient is high.But be not suitable for being easy under the high temperature raw material that decomposes and the production process of product.
Traditional multitube oxidation reactor is fixed bed reactors; This reactor is many reaction tubes that are fixed between the lower perforated plate; Be filled with the catalyst of certain altitude in reaction tube inside; Two kinds of reacting gas mix the back through catalyst bed reaction through preheating, and reaction heat is taken away through the thermophore that circulates in the housing.It is often and ripe that this oxidation reactor is used.
Chinese patent CN200880113893.3 has described the multitube gas phase catalytic oxidation reaction; Two kinds of reacting gas mix the back and concentrate entering mixed air vessel, evenly get in the reaction tube that catalyst is housed then and react, and this structure of reactor has disperseed reaction heat effectively; Avoided the generation of " temperature runaway " phenomenon; Help keeping activity of such catalysts, make to be reflected under the suitable temperature conditions and carry out, the characteristics of this type reaction are that two kinds of unstrpped gases only could be carried out in the presence of catalyst effectively.Therefore two kinds of unstrpped gases that get into mixed air vessel, even reach reaction temperature, if there is not catalyst, it is impossible that oxidation reaction remains.
To sum up; Present multitube gaseous oxidation reduction reactor is not suitable for the temperature height, heat release is strong and the labile gaseous oxidation reduction reaction that does not need catalyst of reacting gas; It is that the synthetic reaction of the carbonyl fluoride of raw material is representative that this type of reaction can be adopted tetrafluoroethene; In this reaction, tetrafluoroethene is prone to polymerization, reacts strong heat release (760.51KJ/mol).
Summary of the invention
The utility model is intended to propose a kind of many endless tubes oxidation reactor, for the gas phase oxidation that does not need catalyst better controlled can be arranged, and such reaction has the temperature height, heat release is strong and the easy characteristics of decomposing, not needing catalyst of reacting gas.For this reason, the utility model adopts following technical scheme:
A kind of multitube oxidation reactor is used for gas phase oxidation, comprises reactor shell, following three parts in it is characterized in that providing in the reactor shell, and said bottom is that reaction gas distribution district, middle part are that reaction zone, top are the product gas heat transfer zone;
The inherent product gas heat transfer zone of said reactor shell below is provided with the many sleeve pipes parallel with the reactor shell longitudinal axis, and said many sleeve pipes distribute on the cross section of reactor shell;
Said reaction gas distribution district is used for two kinds of reacting gas difference mean allocation to each sleeve pipe; Pipe and outer tube in said sleeve pipe comprises; Interior pipe is used for logical first kind of reacting gas; Annular space between interior pipe and the outer tube is used for logical second kind of reacting gas; Said reaction gas distribution district comprises the dispensing zone of first kind of reacting gas and the dispensing zone of second kind of reacting gas, is spaced between the dispensing zone of the dispensing zone of first kind of reacting gas and second kind of reacting gas;
Said outer tube is higher than interior pipe, forms two kinds of reaction zones that reacting gas converges in its raised area.
On the basis of adopting technique scheme, the utility model also can adopt following further technical scheme:
The top of said outer tube is contraction mouth or straight mouth, and said contraction mouth forms gas nozzle.
The top of pipe is contraction mouth or straight mouth in said, preferably adopts contraction mouth.
The dispensing zone of the dispensing zone of said first kind of reacting gas and second kind of reacting gas disposes up and down; Separate by first tube sheet between them; The dispensing zone of first kind of reacting gas is under first tube sheet; Pipe is fixed on first tube sheet and with the dispensing zone of first kind of reacting gas and communicates in said, above said first tube sheet, is provided with second tube sheet in the said reactor shell, and the dispensing zone of second kind of reacting gas is between first tube sheet and second tube sheet; Said outer tube is fixed on second tube sheet, and said annular space communicates with the dispensing zone of second kind of reacting gas.
The inlet of pipe and outer tube is straight tube or horn mouth in said.
Adopt distribution of gas nozzle or gas distributor air inlet in the dispensing zone of the dispensing zone of first kind of reacting gas and second kind of reacting gas.
Said product gas heat transfer zone adopts shell-and-tube heat exchanger, and tube side leads to said product gas, shell side admittance hot body medium.
Reactor shell outside position, said reaction gas distribution district and the reaction zone position is provided with the chuck heat exchanger outward; The media outlet of said chuck heat exchanger links to each other with the medium inlet of shell-and-tube heat exchanger through pipeline, and the media outlet of said shell-and-tube heat exchanger links to each other with the medium inlet of chuck heat exchanger through pipeline.
Said two strands of reacting gas are respectively oxygen molecule or oxidizing gas and the organic or inorganic gas that need be reacted.The reaction heat of said gas phase oxidation is 10-1000KJ/kmol.
Said gas phase oxidation be tetrafluoroethene be raw material carbonyl fluoride synthetic reaction or with the reaction of chlorine and combustion of hydrogen system hydrogen chloride.
Because adopt the technical scheme of the utility model, the utility model solves the even distribution of reacting gas dexterously, can realize the internal combustion reaction of two gases in the specific region, reaction heat energy is in time taken away, and the conversion ratio of oxidation reaction and selectivity are higher.Be particularly suitable for high such as the synthetic reaction equitemperature of carbonyl fluoride that with the tetrafluoroethene is raw material, heat release strong and the labile gas phase oxidation that does not need catalyst of reacting gas.
The reactor that the utility model provided adopts many endless tubes of shell-and-tube parallel way; Wherein a kind of unstrpped gas is directly sent into interior endless tube; Another kind of gas is sent into annular space; Assurance is reflected at the sleeve pipe top to be carried out, and a large amount of heats that reaction produces are removed rapidly, and oxidation reaction is carried out in the atmosphere that relatively relaxes.Reaction simultaneously can obtain high conversion ratio and selectivity.
Description of drawings
Fig. 1 is the sketch map of the utility model reactor embodiment 1.
Fig. 2 is the sketch map of the utility model reactor embodiment 2.
Fig. 3 is the enlarged drawing at I position among Fig. 1, shows a kind of embodiment at sleeve pipe top.
Fig. 4 is the enlarged drawing at I position among Fig. 1, shows the another kind of embodiment at sleeve pipe top.
The specific embodiment
Embodiment 1, with reference to accompanying drawing 1,3,4.
The multitube oxidation reactor that the utility model provided; Being used for gas phase oxidation, is the oxidation reaction that the synthetic reaction of the carbonyl fluoride of raw material does not need catalyst with the reaction and the various organic and inorganic gas of chlorine and combustion of hydrogen system hydrogen chloride such as tetrafluoroethene.Said reactor comprises reactor shell 1, following three parts in providing in the reactor shell, and said bottom is that reaction gas distribution district, middle part are that reaction zone, top are the product gas heat transfer zone;
Said reactor shell 1 inherent product gas heat transfer zone below is provided with the many sleeve pipes parallel with the reactor shell longitudinal axis, and said many sleeve pipes distribute on the cross section of reactor shell;
Said reaction gas distribution district is used for two kinds of reacting gas difference mean allocation to each sleeve pipe; Pipe 21 and outer tube 22 in said sleeve pipe comprises, interior pipe are used for logical first kind of reacting gas, and the annular space 23 between interior pipe 21 and the outer tube 22 is used for logical second kind of reacting gas, and interior pipe gas and annular space gas can be changed each other.Said reaction gas distribution district comprises between the dispensing zone of dispensing zone 100 and second kind of reacting gas 200 of 200, the first kinds of reacting gas of dispensing zone of dispensing zone 100 and second kind of reacting gas of first kind of reacting gas and being spaced;
Pipe 21 in said outer tube 22 is higher than forms two kinds of reaction zones 24 that reacting gas converges in its raised area.
The dispensing zone 100 of said first kind of reacting gas and the dispensing zone 200 of second kind of reacting gas dispose up and down; Separate by first tube sheet 3 between them; The dispensing zone 21 of first kind of reacting gas is under first tube sheet 3; Pipe 21 is fixed on first tube sheet 3 and with the dispensing zone 100 of first kind of reacting gas and communicates in said, is between first tube sheet 3 and second tube sheet 4 in the dispensing zone 200 that is provided with 4, the second kinds of reacting gas of second tube sheet above said first tube sheet in the said reactor shell; Said outer tube 22 is fixed on second tube sheet 4, and said annular space 23 communicates with the dispensing zone 200 of second kind of reacting gas.
As shown in Figure 4, the top of outer tube 22 can be contraction mouth 24, and contraction mouth 24 forms gas nozzle, also or at the top of outer tube 22 gas nozzle is installed, and as shown in Figure 3, the top of outer tube 22 also can be undressed cylindrical.Interior pipe 21 tops are undressed cylindrical tube faces, also treated contraction mouth.The inlet of pipe 21 and outer tube 22 all can be horn mouth in said.In pipe 21 can select all kinds of stainless steel tubes for use with the material of outer tube 22, best 304 stainless steel tubes of selecting for use.The caliber of interior pipe and outer tube is too big, and reaction heat can not effectively remove, the poor selectivity of reaction; Reaction tube is directly selected too little, and the quantity of reaction tube can greatly increase, and reactor processed complex, overall volume strengthen, and in general, the diameter of interior pipe 21 and outer tube 22 can be selected in 0.3mm between the 30mm.
For guaranteeing a large amount of reacting gas homogeneous reaction in reactor; To guarantee that at first two kinds of gas flow and proportionings on demand of participating in reaction get into reactor respectively; Two strands of raw materials that get into reactor according to quantity are earlier through anticipatory electric heater heating or conduction oil preheating, and this dual mode is shared or select one of which to carry out preheating.But can not make any gas in the process of preheating, produce decomposition, polymerization or explosion danger.Blast wall need be set under the situation about being necessary or safety devices such as rupture disk are set to reactor.
The utility model has designed the dispensing zone of gas respectively to two kinds of reacting gas in reactor, this is intended to unstrpped gas and cushions herein.Use suitable gas distributor when the air inlet for two kinds of reacting gas; Can avoid gas to produce and concentrate stream or dispersion train; For this reason; In the utility model, in the dispensing zone of the dispensing zone of first kind of reacting gas and second kind of reacting gas, can adopt the air inlet of distribution of gas nozzle, they can be in the centre position of corresponding dispensing zone.
Whole oxidation reaction can be reacted under the condition of normal pressure or pressurization, and the diameter of reactor can be 50～5000mm, and the distribution radical of sleeve pipe is can be to 3000; Sleeve pipe quantity for a long time; The combustion zone heat can not be too concentrated, and therefore, preferably the centre-to-centre spacing of every sleeve pipe is between 10～50mm.
After two strands of gases of reaction were reaching the certain reaction temperature, reaction caused at once, and utilized the reaction heat of self, kept carrying out continuously of reaction.If adopt the such reactor of similar Chinese patent CN200880113893.3, two kinds of reaction raw materials gases mix the back to be concentrated and gets into inlet plenums, in the reaction tube of preheating, receive thermal booster reaction after; Conversion zone can extend back along air-flow incoming road direction, in spreading back concentrated inlet plenum, takes place " tempering "; Cause more violent reaction; Because reaction heat can not be removed effectively, can burn reactor when serious, even blast.
How to control the taking-up problem of heat of reaction well, not only be related to safe problem, the yield problem to product also is to be worth exploring simultaneously.Reaction heat is untimely to be removed, and can make reaction continue at high temperature to carry out secondary response or generation temperature runaway, produces too much impurity, is unfavorable for the separation of back system.
For this reason, the utility model with the same cylindrical shell of reaction zone above be provided with the product gas heat transfer zone.
In the present embodiment, said product gas heat transfer zone adopts shell-and-tube heat exchanger, and said product gas is walked tube side, and shell side feeds the heat carrier medium.Drawing reference numeral 51 is the runner pipe of product gas.Misphase is equipped with multilayer deflection plate 52 on the runner pipe.
The heat carrier medium that is used for gas converting heat of shell-and-tube heat exchanger can be selected water, conduction oil or other organic solvents, and best choice is a conduction oil, and conduction oil can be realized circulation through power-equipment, and intermediate link is provided with oily temperature stabilization element.
Oxygen molecule or the oxidizing gas of participating in reaction with need all need to be passed through the outside and be preheating to certain temperature and could get into reactor by the organic or inorganic gas of fully reaction.The gas preheat temperature can be controlled in 250～350 ℃.
Before carrying out oxidation reaction, reactor need carry out preheating, and the reactor preheating can be carried out through heated nitrogen, keeps internal temperature to reach 200～350 ℃.The nitrogen of said heating feeds the dispensing zone 100 of first kind of reacting gas and the dispensing zone of second kind of reacting gas 200, gets into reaction zone through sleeve pipe, through the tube side of heat transfer zone, flows out from the product gas outlet 11 at reactor shell top again.
Embodiment 2, with reference to Fig. 2.
In the present embodiment, the preheating method of reactor has been selected for use another kind of mode, this mode can with the shell-and-tube heat exchanger operation that combines, their shared heat carrier media are to make full use of reaction heat, energy savings.
Reactor shell outside position, said reaction gas distribution district and the reaction zone position is provided with chuck heat exchanger 6 outward; The media outlet 61 of said chuck heat exchanger links to each other with the medium inlet 53 of shell-and-tube heat exchanger through pipeline; The media outlet 54 of said shell-and-tube heat exchanger links to each other with the medium inlet 62 of chuck heat exchanger 6 through pipeline, in the middle of pipeline, valve, pump, temperature stabilization unit etc. can be set.
Other part of present embodiment is identical with embodiment 1, in Fig. 2, and drawing reference numeral and Fig. 1,3,4 identical identical implications of representative.
Claims (10)
1. a multitube oxidation reactor is used for gas phase oxidation, comprises reactor shell, following three parts in it is characterized in that providing in the reactor shell, and said bottom is that reaction gas distribution district, middle part are that reaction zone, top are the product gas heat transfer zone;
The inherent product gas heat transfer zone of said reactor shell below is provided with the many sleeve pipes parallel with the reactor shell longitudinal axis, and said many sleeve pipes distribute on the cross section of reactor shell;
Said reaction gas distribution district is used for two kinds of reacting gas difference mean allocation to each sleeve pipe; Pipe and outer tube in said sleeve pipe comprises; Interior pipe is used for logical first kind of reacting gas; Annular space between interior pipe and the outer tube is used for logical second kind of reacting gas; Said reaction gas distribution district comprises the dispensing zone of first kind of reacting gas and the dispensing zone of second kind of reacting gas, is spaced between the dispensing zone of the dispensing zone of first kind of reacting gas and second kind of reacting gas;
Said outer tube is higher than interior pipe, forms two kinds of reaction zones that reacting gas converges in its raised area.
2. a kind of multitube oxidation reactor as claimed in claim 1, the top that it is characterized in that said outer tube is a contraction mouth, said contraction mouth forms gas nozzle.
3. according to claim 1 or claim 2 a kind of multitube oxidation reactor, it is characterized in that said in the top of pipe be contraction mouth.
4. a kind of multitube oxidation reactor as claimed in claim 1; It is characterized in that the dispensing zone of said first kind of reacting gas and the dispensing zone of second kind of reacting gas dispose up and down; Separated by first tube sheet between them, the dispensing zone of first kind of reacting gas is under first tube sheet, and said interior pipe is fixed on first tube sheet and with the dispensing zone of first kind of reacting gas and communicates; Above said first tube sheet, be provided with second tube sheet in the said reactor shell; The dispensing zone of second kind of reacting gas is between first tube sheet and second tube sheet, and said outer tube is fixed on second tube sheet, and said annular space communicates with the dispensing zone of second kind of reacting gas.
5. like claim 1 or 4 described a kind of multitube oxidation reactors, it is characterized in that the inlet of said interior pipe and outer tube is horn mouth.
6. like claim 1 or 4 described a kind of multitube oxidation reactors, it is characterized in that adopting the air inlet of distribution of gas nozzle in the dispensing zone of dispensing zone and second kind of reacting gas of first kind of reacting gas.
7. a kind of multitube oxidation reactor as claimed in claim 1 is characterized in that said product gas heat transfer zone adopts shell-and-tube heat exchanger, and tube side leads to said product gas, shell side admittance hot body medium.
8. a kind of multitube oxidation reactor as claimed in claim 7; It is characterized in that the reactor shell outside position, said reaction gas distribution district and the reaction zone position is provided with the chuck heat exchanger outward; The media outlet of said chuck heat exchanger links to each other with the medium inlet of shell-and-tube heat exchanger through pipeline, and the media outlet of said shell-and-tube heat exchanger links to each other with the medium inlet of chuck heat exchanger through pipeline.
9. a kind of multitube oxidation reactor as claimed in claim 1 is characterized in that said two strands of reacting gas are respectively oxygen molecule or oxidizing gas and the organic or inorganic gas that need be reacted; The reaction heat of said gas phase oxidation is 10-1000KJ/kmol.
10. a kind of multitube oxidation reactor as claimed in claim 1, it is characterized in that said gas phase oxidation be tetrafluoroethene be raw material carbonyl fluoride synthetic reaction or with the reaction of chlorine and combustion of hydrogen system hydrogen chloride.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011205685280U CN202447060U (en) | 2011-12-30 | 2011-12-30 | Multi-tube oxidation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011205685280U CN202447060U (en) | 2011-12-30 | 2011-12-30 | Multi-tube oxidation reactor |
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| Publication Number | Publication Date |
|---|---|
| CN202447060U true CN202447060U (en) | 2012-09-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011205685280U Expired - Lifetime CN202447060U (en) | 2011-12-30 | 2011-12-30 | Multi-tube oxidation reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102527301A (en) * | 2011-12-30 | 2012-07-04 | 中化蓝天集团有限公司 | Multi-tube oxidation reactor |
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2011
- 2011-12-30 CN CN2011205685280U patent/CN202447060U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102527301A (en) * | 2011-12-30 | 2012-07-04 | 中化蓝天集团有限公司 | Multi-tube oxidation reactor |
| CN102527301B (en) * | 2011-12-30 | 2014-01-29 | 中化蓝天集团有限公司 | Multi-tube oxidation reactor |
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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: 20120926 Effective date of abandoning: 20140129 |
|
| RGAV | Abandon patent right to avoid regrant |