CN206064374U - For high concentration alkynes and the calandria type fixed bed reactor of alkadienes - Google Patents
For high concentration alkynes and the calandria type fixed bed reactor of alkadienes Download PDFInfo
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- CN206064374U CN206064374U CN201620987023.0U CN201620987023U CN206064374U CN 206064374 U CN206064374 U CN 206064374U CN 201620987023 U CN201620987023 U CN 201620987023U CN 206064374 U CN206064374 U CN 206064374U
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Abstract
The utility model discloses a kind of for high concentration alkynes and the calandria type fixed bed reactor of alkadienes, the reactor is calandria type fixed bed reactor, constitute including housing, tubulation, the feature mouth of pipe and internals etc., the common hydrogenation catalyst of filling solid in tubulation, is hydrogenated with altogether for carrying out selectivity to mixing carbon four.The reactor main function mouth of pipe and internals include：Many specification porcelain ball, inlet dispenser, outlet collector, discharge port, charging aperture, circulation port, water inlet, outlet, relief valve port, discharging opening, air vent and drain.The conversion ratio that this utility model can solve the selective hydrogenation that traditional device is present is low, and equipment volume is big, reactor produce because of drastically temperature runaway coking etc. technical problem.
Description
Technical field
The present invention relates to a kind of petroleum refining equipment, more particularly to one kind are applied to mixing four selectivity of carbon is hydrogenated with dress altogether
Put.
Background technology
Mixing carbon four is important petrochemical industry resource, and the refinery gas and petroleum hydrocarbon for coming from petroleum refining process generation splits
The side-product of solution process of producing ethylene.Mixing carbon four mainly contains normal butane, iso-butane, 1-butylene, Trans-2-butene, cis- 2- fourths
Alkene, isobutene., 1,2- butadiene, 1,3- butadiene, allylene, ethyl acetylene, vinylacetylene etc. are full to close hydrocarbon and unsaturation
Hydrocarbon, is industrially mainly used to produce isobutene. and 1-butylene.
1-butylene is one of important basic chemical industry raw material, is synthesis sec-butyl alcohol, the raw material of dehydrogenation butadiene.With formaldehyde
Reaction generates isoprene, can be made into the polyisobutylene polymer of different molecular weight for use as lube oil additive, resin etc., water
Preparing tert-butanol is closed, the monomers methyl methacrylate of lucite processed is aoxidized.
Isobutene. is a kind of important petrochemical materials, and industrial high concentration isobutene. is mainly for the production of polyisobutylene
And butyl rubber is produced with isoprene copolymer.Isobutene. is alkylated reaction with iso-butane, can produce high-octane rating alkane
Base gasoline, it is excellent gasoline additive to react gained methyl tertiary butyl ether(MTBE) with methanol.It is also applied for making the alkylation of aromatic hydrocarbons
Raw material, or the fine chemicals of the operation production such as oxidized, ammonification.The derivant 2- tertiary butyl paracresol of isobutene. and 2- nitre
Base -5- chloroaniline diazonium compound is coupled, and then reduction can obtain 2,3' tertiary butyl -2' hydroxyl -5'- aminomethyl phenyl -5- chlorobenzenes three
Azoles, is good UV absorbent.Also o- t-butyl phenol Jing is nitrified and can be obtained 2- tertiary butyl -4,6- dinitrophenol,DNP, it
It is agricultural herbicide, is widely used in the departments such as light industry, oil refining, medicine, spice, building materials and other fine chemistry industries.
Therefore, to mix carbon four carry out selective hydrogenation, by 1，2-butadiene therein, 1,3-butadiene, allylene,
The diolefins such as ethyl acetylene, vinylacetylene and alkynes are hydrogenated to isobutene. and 1-butylene, can effectively improve mixing carbon four
Value.
The conversion ratio that traditional common hydrogenation plant of four selectivity of mixing carbon has selective hydrogenation is low, and equipment volume is big,
Reactor produce because of drastically temperature runaway coking the problems such as.
The content of the invention
It is an object of the invention to provide it is a kind of for high concentration alkynes and the calandria type fixed bed reactor of alkadienes, to solve
The conversion ratio of the selective hydrogenation that certainly traditional device is present is low, and equipment volume is big, and reactor produces coking because of drastically temperature runaway
Etc. technical problem.
In order to solve foregoing invention purpose, the technology used in the present invention problem is as follows：
For high concentration alkynes and the calandria type fixed bed reactor of alkadienes, the reactor is calandria type fixed bed reaction
Device, including housing, tubulation, the feature mouth of pipe and internals；Load in tubulation for carrying out what selectivity was hydrogenated with altogether to mixing carbon four
The common hydrogenation catalyst of solid；The reactor feature mouth of pipe and internals include：Many specification porcelain ball, inlet dispenser, outlet collection
Clutch, discharge port, charging aperture, circulation port, water inlet, outlet, relief valve port, discharging opening, air vent and drain；For
Support solid in tubulation altogether hydrogenation catalyst, and described many specification porcelain ball of distribution effect are played with multi-tier arrangement in reaction
Device bottom；Be located at the foot of reactor for the equally distributed inlet dispenser into reactor content, and with it is outside
Charging aperture is connected；Collecting and intercept solid catalyst particle for reactor outlet material, it is to avoid the outlet set of loss
Device is located at the top of reactor, and is connected with outside discharging opening；For drawing off many specification porcelain ball in reactor and consolidating
The discharge port of the common hydrogenation catalyst of body is located at the bottom of reactor low head；Wait that the charging aperture for being hydrogenated with mixing four raw material of carbon is located at anti-
The bottom of device is answered, and is connected with internal inlet dispenser；Reactor outlet be hydrogenated with altogether after material, a part therein carries out
Circulation, is entered by circulation port, and is connected with outside charging aperture；By the cooling water between tubulation, add for removing reactor
The water inlet of the cooling water of the reaction heat produced during hydrogen is located at lower housing portion；The outlet of cooling water used by reactor is located at housing
Top；Relief valve port is located at reactor top；The discharging opening for mixing four product of carbon after hydrogenation is located at reactor top；For discharging
Fixed gas, makes cooling water full of housing and tubulation gap, it is ensured that the air vent for cooling down completely of tubulation is located at the top of housing；
Drain for the cooling water in emptying housing and tubulation gap is located at the top of housing.
Solid catalyst is the metallic catalyst loaded on aluminium oxide or molecular sieve.
Solid catalyst includes palladio, platinum based noble metal catalyst.
The arrangement mode of tubulation includes in equilateral triangle, square, corner equilateral triangle or corner square mode one
Kind.
Many specification porcelain ball, it is ascending by diameter, order multi-tier arrangement from top to bottom in hydrogenation reactor bottom,
The porcelain ball number of plies be N shell, 1≤N≤10；A diameter of 2～the Φ of Φ of porcelain ball 100.
The porcelain ball number of plies preferably 2≤N≤5, the preferred 3～Φ of Φ of the porcelain ball diameter 20.
Advantages of the present invention and good effect are as follows：1st, compact conformation, saves space and investment, is easy to operate and manages；
2nd, inlet dispenser and outlet collector are provided with reactor cylinder body, can have both realized being uniformly distributed for feed stream,
Solid catalyst particle can be intercepted again, it is to avoid be lost in；3rd, the reaction heat produced when reactor is hydrogenated with, can be by between tubulation
Cooling water is removed；4th, air speed is improve, saves catalyst, reduce circulating load.Operation is more flexible, safe and reliable,
Hydrogenation conversion is high altogether for selectivity, is prevented effectively from the reactor drastically situation such as temperature runaway, coking.
Description of the drawings
Fig. 1 is the structural representation of the present invention.
Fig. 2 is sectional views along A-A direction of the Fig. 1 by taking the arrangement mode of tubulation equilateral triangle as an example.
Fig. 3 is the structural representation of the outlet collector of the present invention.
Fig. 4 is the B of Fig. 3 to structural representation.
Fig. 5 is the structural representation of the inlet dispenser of the present invention.
Fig. 6 is the C of Fig. 5 to structural representation.
Number in figure：1st, reactor shell；2nd, tubulation；3rd, many specification porcelain ball；4th, inlet dispenser；4-1, inlet dispenser
Bar hole；The circular port of 4-2, inlet dispenser；5th, outlet collector；The bar hole of 5-1, outlet collector；5-2, outlet
The circular hole of collector；6th, discharge port；7th, charging aperture；8th, circulation port；9th, water inlet；10th, outlet；11st, relief valve port；12nd, go out
Material mouth；13rd, air vent；14th, drain.
Specific embodiment
The concrete structure of the present invention is referring to shown in Fig. 1,2.For the calandria type fixed bed anti-of high concentration alkynes and alkadienes
Device is answered, the reactor is calandria type fixed bed reactor, including housing 1, tubulation 2, the feature mouth of pipe and internals；Fill in tubulation 2
Fill out for carrying out the common hydrogenation catalyst of solid that selectivity is hydrogenated with altogether to mixing carbon four；The reactor feature mouth of pipe and internals
Including：Many specification porcelain ball 3, inlet dispenser 4, outlet collector 5, discharge port 6, charging aperture 7, circulation port 8, water inlet 9, water outlet
Mouth 10, relief valve port 11, discharging opening 12, air vent 13 and drain 14；For supporting the hydrogenation catalyst altogether of the solid in tubulation,
And described many specification porcelain ball 3 of distribution effect are played with multi-tier arrangement in reactor lower part；For into reactor content
Equally distributed inlet dispenser 4 is located at the foot of reactor, and is connected with outside charging aperture 7；Go out for reactor
Mouthful material collects and intercepts solid catalyst particle, it is to avoid the outlet collector 5 of loss positioned at the top of reactor, and with
Outside discharging opening 12 is connected；For drawing off the discharge port 5 of many specification porcelain ball in reactor and the common hydrogenation catalyst of solid
Positioned at the bottom of reactor low head；Wait that the charging aperture 7 for being hydrogenated with mixing four raw material of carbon is located at the bottom of reactor, and with it is internal
Inlet dispenser 4 is connected；Reactor outlet be hydrogenated with altogether after material, a part therein is circulated, entered by circulation port 8,
And be connected with outside charging aperture 7；By the cooling water between tubulation 2, for removing the reaction heat produced when reactor is hydrogenated with
Cooling water water inlet 9 be located at 1 bottom of housing；The outlet 10 of cooling water used by reactor is located at 1 top of housing；Relief valve
Mouth 11 is located at reactor top；The discharging opening 12 for mixing four product of carbon after hydrogenation is located at reactor top；For discharging fixed gas,
Cooling water is made full of housing 1 and 2 gap of tubulation, it is ensured that the air vent 13 for cooling down completely of tubulation 2 is located at the top of housing 1；
Drain 14 for the cooling water in emptying housing and tubulation gap is located at the top of housing 1.
Solid catalyst is the metallic catalyst loaded on aluminium oxide or molecular sieve, including the noble metal such as palladio, platino is urged
Agent.
The arrangement mode of tubulation 2 mainly includes the modes such as equilateral triangle, square, corner equilateral triangle, corner square.
Many specification porcelain ball 3, ascending by diameter, order multi-tier arrangement from top to bottom is in hydrogenation reactor bottom
Portion, the porcelain ball number of plies be N shell, 1≤N≤10, preferably 2≤N≤5；A diameter of 2～the Φ of Φ 100 of porcelain ball, preferred 3～Φ of Φ 20.
The course of work：
(1) four raw material of mixing carbon of alkynes containing high concentration and alkadienes enters reactor, Jing inlet dispensers from charging aperture 7
4 and many specification porcelain ball 3, into the tubulation 2 in reactor, common hydrogenation reaction is carried out under catalyst action.
(2) reactor cooling water water inlet 9 and 10 regulating valve of outlet are adjusted according to temperature of reactor situation, it is ensured that reaction
The temperature of device is normal.
(3) the material Jing outlet collectors 5 after reactor hydrogenation, discharge from discharging opening 12, and a portion is entered
Next operation, 8 Returning reactor of another part self-loopa mouth, with the alkynes containing high concentration and alkadienes entered from charging aperture 7
Four raw material of mixing carbon mixing after, continuation reacted in the reactor.
(4) when catalyst is inactivated or reaches service life, self-unloading material mouth 6 draws off.
By the reactor of the present invention, four raw material of mixing carbon (table 1) to following composition, a kind of common hydrogenation catalyst of solids of Jing
Agent is acted on, and four selectivity of mixing carbon for carrying out high concentration alkynes and alkadienes is hydrogenated with altogether, can be by the diolefin in mixing carbon four, alkynes
Hydrocarbon, is changed into monoolefine by common hydrogenation plant, and after final hydrogenation, product index is：Mixing insatiable hunger of the carbon four in addition to monoolefine
With alkynes and unsaturated olefin total content≤100ppm.
The mixing carbon four raw materials composition of table 1
| Sequence number | Title | Content (w%) |
| 1 | Vinylacetylene | 0～0.3 |
| 2 | Ethyl acetylene | 0～0.04 |
| 3 | Allylene | 0～0.09 |
| 4 | Ethyl acetylene | 0～0.1 |
| 5 | 1,3- butadiene | 0～0.4 |
| 6 | 1,2- butadiene | 0～0.1 |
| 7 | Monoolefine and C4 alkane | Surplus |
Claims (6)
1. the calandria type fixed bed reactor of high concentration alkynes and alkadienes is used for, it is characterised in that the reactor is shell and tube
Fixed bed reactors, including housing, tubulation, the feature mouth of pipe and internals；Load in tubulation for selecting to mixing carbon four
Property the solid that is hydrogenated with altogether hydrogenation catalyst altogether；The reactor feature mouth of pipe and internals include：Many specification porcelain ball, entrance distribution
Device, outlet collector, discharge port, charging aperture, circulation port, water inlet, outlet, relief valve port, discharging opening, air vent and put net
Mouthful；For supporting the hydrogenation catalyst altogether of the solid in tubulation, and described many specification porcelain ball of distribution effect are played with laminates
It is placed in reactor lower part；The foot of reactor is located at for the equally distributed inlet dispenser into reactor content, and
It is connected with outside charging aperture；Collecting and intercept solid catalyst particle for reactor outlet material, it is to avoid loss
Outlet collector is located at the top of reactor, and is connected with outside discharging opening；For drawing off many specifications in reactor
The discharge port of porcelain ball and the common hydrogenation catalyst of solid is located at the bottom of reactor low head；Wait to be hydrogenated with the charging of mixing four raw material of carbon
Mouth is located at the bottom of reactor, and is connected with internal inlet dispenser；Reactor outlet be hydrogenated with altogether after material, therein one
Part is circulated, and is entered by circulation port, and is connected with outside charging aperture；By the cooling water between tubulation, for removing
The water inlet of the cooling water of the reaction heat that reactor is produced when being hydrogenated with is located at lower housing portion；The outlet of cooling water used by reactor
Positioned at housing upper；Relief valve port is located at reactor top；The discharging opening for mixing four product of carbon after hydrogenation is located at reactor top；
For discharging fixed gas, cooling water is made full of housing and tubulation gap, it is ensured that the air vent for cooling down completely of tubulation is located at housing
The top；Drain for the cooling water in emptying housing and tubulation gap is located at the top of housing.
2. according to claim 1 for high concentration alkynes and the calandria type fixed bed reactor of alkadienes, its feature exists
In solid catalyst is the metallic catalyst loaded on aluminium oxide or molecular sieve.
3. according to claim 2 for high concentration alkynes and the calandria type fixed bed reactor of alkadienes, its feature exists
In solid catalyst includes palladio, platinum based noble metal catalyst.
4. according to claim 1 for high concentration alkynes and the calandria type fixed bed reactor of alkadienes, its feature exists
In the arrangement mode of tubulation includes the one kind in equilateral triangle, square, corner equilateral triangle or corner square mode.
5. according to claim 1 for high concentration alkynes and the calandria type fixed bed reactor of alkadienes, its feature exists
In, many specification porcelain ball, ascending by diameter, order multi-tier arrangement from top to bottom is in hydrogenation reactor bottom, described
The porcelain ball number of plies be N shell, 1≤N≤10；A diameter of 2～the Φ of Φ of porcelain ball 100.
6. according to claim 5 for high concentration alkynes and the calandria type fixed bed reactor of alkadienes, its feature exists
In, the porcelain ball number of plies 2≤N≤5,3～Φ of the porcelain ball diameter of phi 20.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620987023.0U CN206064374U (en) | 2016-08-30 | 2016-08-30 | For high concentration alkynes and the calandria type fixed bed reactor of alkadienes |
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| CN201620987023.0U CN206064374U (en) | 2016-08-30 | 2016-08-30 | For high concentration alkynes and the calandria type fixed bed reactor of alkadienes |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106179132A (en) * | 2016-08-30 | 2016-12-07 | 凯瑞环保科技股份有限公司 | A kind of mixing carbon four selectivity for high concentration alkynes and alkadienes is hydrogenated with calandria type fixed bed reactor altogether |
| CN110624480A (en) * | 2018-06-22 | 2019-12-31 | 中国石油化工股份有限公司 | Fixed bed reactor and unsaturated light hydrocarbon hydrogenation method |
-
2016
- 2016-08-30 CN CN201620987023.0U patent/CN206064374U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106179132A (en) * | 2016-08-30 | 2016-12-07 | 凯瑞环保科技股份有限公司 | A kind of mixing carbon four selectivity for high concentration alkynes and alkadienes is hydrogenated with calandria type fixed bed reactor altogether |
| CN110624480A (en) * | 2018-06-22 | 2019-12-31 | 中国石油化工股份有限公司 | Fixed bed reactor and unsaturated light hydrocarbon hydrogenation method |
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