CN106732311A - A kind of spherical cavity header coil pipe reactor of water route Natural Circulation - Google Patents
A kind of spherical cavity header coil pipe reactor of water route Natural Circulation Download PDFInfo
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- CN106732311A CN106732311A CN201710050378.6A CN201710050378A CN106732311A CN 106732311 A CN106732311 A CN 106732311A CN 201710050378 A CN201710050378 A CN 201710050378A CN 106732311 A CN106732311 A CN 106732311A
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- Prior art keywords
- pipe
- header
- water
- inflator
- catalyst
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 96
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 118
- 239000003054 catalyst Substances 0.000 claims abstract description 55
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 31
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 25
- 230000008676 import Effects 0.000 claims abstract description 8
- 238000000034 method Methods 0.000 claims description 13
- WCCJDBZJUYKDBF-UHFFFAOYSA-N copper silicon Chemical compound [Si].[Cu] WCCJDBZJUYKDBF-UHFFFAOYSA-N 0.000 claims description 3
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 claims description 3
- 150000002940 palladium Chemical class 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 abstract description 10
- 230000006315 carbonylation Effects 0.000 abstract description 6
- 238000005810 carbonylation reaction Methods 0.000 abstract description 6
- 230000008646 thermal stress Effects 0.000 abstract description 6
- 230000007547 defect Effects 0.000 abstract description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 45
- 238000006243 chemical reaction Methods 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- 238000007086 side reaction Methods 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- BLLFVUPNHCTMSV-UHFFFAOYSA-N methyl nitrite Chemical compound CON=O BLLFVUPNHCTMSV-UHFFFAOYSA-N 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 206010011906 Death Diseases 0.000 description 2
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 2
- 241000270295 Serpentes Species 0.000 description 2
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 description 2
- 230000008030 elimination Effects 0.000 description 2
- 238000003379 elimination reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 125000003827 glycol group Chemical group 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 1
- 238000010685 alcohol synthesis reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011982 device technology Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000010117 shenhua Substances 0.000 description 1
- 230000035882 stress Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/002—Avoiding undesirable reactions or side-effects, e.g. avoiding explosions, or improving the yield by suppressing side-reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00081—Tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00245—Avoiding undesirable reactions or side-effects
- B01J2219/00259—Preventing runaway of the chemical reaction
- B01J2219/00263—Preventing explosion of the chemical mixture
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/00718—Type of compounds synthesised
- B01J2219/0072—Organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/2402—Monolithic-type reactors
- B01J2219/2409—Heat exchange aspects
- B01J2219/2411—The reactant being in indirect heat exchange with a non reacting heat exchange medium
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The invention discloses a kind of spherical cavity header coil pipe reactor of water route Natural Circulation, including pressure-bearing shell, catalyst framework and heat-exchanging tube bundle, the catalyst framework and heat-exchanging tube bundle are separately positioned in pressure-bearing shell；The heat-exchanging tube bundle includes outlet pipe, spherical cavity of catchmenting header, coiled pipe, point water polo chamber header and water inlet pipe, the outlet pipe is arranged on the top of pressure-bearing shell, one end of the spherical cavity header that catchments connects the import of outlet pipe, the other end is connected by branch pipe with the outlet of coiled pipe, the coiled pipe is distributed along the axial direction of pressure-bearing shell, described point of one end of water polo chamber header connects the import of coiled pipe by branch pipe, and the other end connects the outlet of water inlet pipe, and the water inlet pipe is connected to the bottom of pressure-bearing shell.It is of the invention thoroughly to eliminate thermal stress, the security and stability of carbonylation, hydrogenation, methanol synthesis reactor is effectively improved, easily heat exchanger plates such as easily reveal at the defect in leakage and plate-type reactor to be prevented effectively from shell and tube reactor in the prior art.
Description
Technical field
The present invention relates to a kind of chemical reactor, more particularly to a kind of water route Natural Circulation spherical cavity header coil pipe type
Reactor.
Background technology
Existing hydrogenation reactor is generally shell and tube reactor or plate-type reactor, shell and tube reactor, filling in pipe
It is water that catalyst, pipe are outer.The tubulation of hydrogenation reactor is 45 × 4~φ of φ 70 × 4, the maximum product for commercially having put into operation at present
Can be 100,000 tons of ethylene glycol, hydrogenation reactor specification accomplishes φ 6800HUrge=10000 specification, because thermal stress eliminates not thorough
Bottom, bed resistance is high, and reactor leakage, device is in end-of-life state.The ethylene glycol dress that commercially many places are put into operation
Put, actual monosystem is classified as 50,000 tons of ethylene glycol production capacity, 200,000 tons of hydrogenation reactions of ethylene glycol use two series, four φ
4200、HUrge=6000 hydrogenation reactor parallel running, have that Catalyst packing is few, big, high energy consumption of moving hot ability, resistance,
The defect such as side reaction thing is more, device is difficult to amplify；Leak water in the plate of board-like hydrogenation reactor, the outer loading catalyst of plate, gas are
Full Radial Flow, can meet larger-scale unit glycol unit in theory, hydrogenation reaction is not suitable on Practical Project and is used.By
Carburetting reaction can occur in ethanol and ethylene glycol, if bed overtemperature occurs and easily forms coking.
Enclosed by the cuboid plate of several 150~400 (plate is wide) × H (plate is high) during the heat exchange element of board-like hydrogenation reactor
Into periphery, this periphery is really one polygonal, and catalyst occurs that became uneven is even, is susceptible to beds
, there is coking phenomenon in hot-spot, the actual operation of input of having no idea.
Existing oxonation device is generally shell and tube reactor or plate-type reactor, shell and tube reactor, filling in pipe
It is water that catalyst, pipe are outer.The tubulation of oxonation device is 25 × 2~φ of φ 32 × 2, the maximum product for commercially having put into operation at present
Can be 100,000 tons of ethylene glycol, oxonation device specification accomplishes φ 6000HUrge=8000 specification, because thermal stress is eliminated not thoroughly,
Bed resistance is high, and reactor leakage, device is in end-of-life state.The glycol unit that commercially many places are put into operation,
Actual monosystem is classified as 50,000 tons of ethylene glycol production capacity, and 200,000 tons of oxonations of ethylene glycol use two series, four φ 4600,
HUrge, there is few Catalyst packing, the hot ability of shifting, big resistance, easily high energy consumption, hair in=6000 oxonation device parallel running
Raw decomposition explosion, the defect such as side reaction thing is more, tube sheet easily burns, device is difficult to amplify；
Enclosed by the cuboid plate of several 150~400 (plate is wide) × H (plate is high) during the heat exchange element of board-like oxonation device
Into periphery, this periphery is really one polygonal, and catalyst occurs that became uneven is even, is susceptible to beds
Hot-spot, is not suitable for oxonation and uses on Practical Project, because methyl nitrite begins to occur thermal decomposition instead at 140 DEG C
Should, methyl nitrite will occur to thermally decompose completely at 155~160 DEG C, and it is big that pyrolysis releasing heat occurs
(3216j/g CH3ONO), while being a volume increase reaction (2CH3ONO→CH3OH+CH2O+2NO), temperature and pressure are caused
Power is quickly raised, and certainly will cause the accident generation.
Existing methanol reactor is generally the reaction of shell and tube reactor, plate-type reactor or small tube sheet header tube beam formula
Device, shell and tube reactor, it is water that loading catalyst, pipe are outer in pipe.The tubulation of methanol synthesis reactor be 38 × 2~φ of φ 44 ×
2, the maximum production capacity for commercially having put into operation at present is 400,000 tons of methyl alcohol, and methanol synthesis reactor specification accomplishes φ 4200HUrge=
7000 specification, because thermal stress is eliminated not thoroughly, bed resistance is high, and reactor leakage, shell and tube methanol synthesis reactor meets
Not maximization methanol synthesizer.The domestic maximization methanol device in operation, single series production capacity is 60 or 900,000 tons, reaction
Device is the board-like methanol synthesis reactors of Ka Sali or the small tube sheet header tube beam formula methanol synthesis reactor for wearing dimension, and maximize methyl alcohol
Reactor market is monopolized by foreign technology business.But the country introduces board-like nine sets of the methanol synthesis reactors of Ka Sali, has six sets to let out
Dew (such as long Thailand's energy in the Inner Mongol, Anhui Hua Yi, the new new energy in Inner Mongol), will must urge when overhauling board-like heat exchanger component leak source
Change draws off, and the repair time is more than one month.Wear the domestic introduction ten of small tube sheet header tube beam formula methanol synthesis reactor of dimension
More than set, stringing difficulty is big, and the small side reaction thing of heat exchange area is more, beds overtemperature (such as Shenhua packet header methanol-to-olefins
Purpose methanol synthesis reactor), maximization device is difficult to using two more parallel operations, separate unit methanol synthesis reactor
Maximization.
The content of the invention
It is an object of the invention to overcome the deficiencies in the prior art, there is provided a kind of spherical cavity header snake of water route Natural Circulation
Tubular reactor, stress is eliminated on radial and axial and meets production needs.
The present invention is achieved by the following technical solutions, and the present invention includes pressure-bearing shell, catalyst framework and heat exchanger tube
Beam, the catalyst framework and heat-exchanging tube bundle are separately positioned in pressure-bearing shell；The heat-exchanging tube bundle includes outlet pipe, collection water polo
Chamber header, coiled pipe, point water polo chamber header and water inlet pipe, the outlet pipe are arranged on the top of pressure-bearing shell, the spherical cavity of catchmenting
One end of header connects the import of outlet pipe, and the other end is connected by branch pipe with the outlet of coiled pipe, and the coiled pipe is along pressure-bearing shell
Axial direction distribution, described point of one end of water polo chamber header connect the import of coiled pipe by branch pipe, and the other end connects water inlet pipe and goes out
Mouthful, the water inlet pipe is connected to the bottom of pressure-bearing shell.
Maintainer can respectively enter point water polo chamber header inside and the spherical cavity header that catchments by water inlet pipe and outlet pipe
Inside, completion coiled pipe weld seam maintenance under the premise of catalyst is not drawn off.
The pressure-bearing shell includes upper cover, housing, support platform, low head；The upper cover and housing pass through flange
Connection, the support platform is arranged on low head, and the low head is fixed on the bottom of housing.Pressure-bearing shell is not involved in instead
Should, pressure is primarily subjected to, do not contact high-temperature reacting gas.
Used as one of preferred embodiment of the invention, the upper cover is provided with thermocouple port, delivery port and upper gas port, described
Outlet pipe is arranged in delivery port.
Used as one of preferred embodiment of the invention, the low head is provided with lower gas port, water inlet and catalyst self-unloading mouthful；
The water inlet pipe is arranged in water inlet.
The catalyst framework includes flat cover, outer inflator, interior inflator, chuck and wireway；The flat cover is arranged on and catchments
The top of spherical cavity header, along the axially arranged of housing, the interior inflator is set in outer inflator the outer inflator, and the coiled pipe sets
In the space being placed between outer inflator and interior inflator, there is space, the spherical cavity header that catchments between the outer inflator and housing
With the top and bottom that point water polo chamber header is separately positioned on outer inflator, the chuck is set on point water polo chamber header, described
Chuck is respectively communicated with interior inflator and wireway, and the wireway is connected in lower gas port, described point of water polo chamber header and chuck branch
Support the outlet pipe, flat cover, spherical cavity of catchmenting header, outer inflator, coiled pipe, interior inflator, chuck, wireway, is entered in support platform
Loading catalyst in the space that water pipe is formed.
A kind of method for carrying out hydrogenation reaction or methanol synthesis reaction using described reactor.
The method of the hydrogenation reaction or methanol synthesis reaction, comprises the following steps：
(11) copper silicon systems or copper-zinc system catalyst are loaded in catalyst inframe；
(12) leak water from the bottom to top in coiled pipe, upper gas port enters reacting gas, and catalyst bed is passed radially through by outer inflator
There is hydrogenation reaction or methanol synthesis reaction to interior inflator in layer；
(13) after reacting, the water decalescence in coiled pipe, by the heat after the hydrogenation or methanol synthesis reaction of catalyst inframe
Amount is removed, and gas is then collected by interior inflator, into chuck and the annular space of point water polo chamber header, is then discharged and is taken away through lower gas port
Heat.
A kind of method for carrying out oxonation using described reactor.
The method of the oxonation, comprises the following steps：
(21) palladium series catalyst is loaded in catalyst inframe；
(22) leak water from the bottom to top in coiled pipe, lower gas port enters reacting gas, into chuck and the annular space for dividing water polo chamber header,
Beds to outer inflator are passed radially through by interior inflator, oxonation occurs；
(23) after reacting, the water decalescence in coiled pipe removes the heat after the oxonation of catalyst inframe, gas
Then collected by outer inflator, heat is then discharged and taken away through upper gas port.
It is main heat-exchanging tube bundle that the present invention uses coiled pipe, and thoroughly elimination thermal stress is axially and radially being gone up in coiled pipe tube bank；Adopt
Ensure that gas flows radially across beds with outer inflator and interior inflator technology, the bed resistance≤0.001MPa of oxonation,
Bed resistance≤the 0.005MPa of hydrogenation reaction, the bed resistance≤0.008MPa of methanol synthesis reaction；It is main to use coiled pipe
Heat-exchanging tube bundle, water-intake pipe is outer flat in pipe, and gas flow direction is plumbness with water flow direction；Using drum and coiled pipe pipe
Waterway circulating between beam to follow naturally, and waterway circulating multiplying power is high；It is that main heat-exchanging tube bundle and radial gas are distributed to use coiled pipe
Device technology combines, and loaded catalyst is more, it is strong to move heat energy power；Water polo chamber is divided to join respectively using water inlet pipe and outlet pipe
Case inside and spherical cavity header interior welds sealing of catchmenting, maintainer can respectively enter a point water polo by water inlet pipe and outlet pipe
Inside chamber header inside and the spherical cavity header that catchments, the maintenance of coiled pipe weld seam is completed on the premise of catalyst is not drawn off.
The present invention has advantages below compared to existing technology：
1st, thoroughly elimination thermal stress is axially and radially being gone up in coiled pipe tube bank of the present invention, effectively improves carbonylation, hydrogenation, methyl alcohol and closes
Into the security and stability of reactor, heat exchange in the easy leakage of shell and tube reactor in the prior art and plate-type reactor is prevented effectively from
The defects such as the easy leakage of plate；
2nd, the technology combined using outer inflator and interior inflator ensures that gas flows radially across beds, effectively reduces carbonyl
Change, hydrogenation reaction and methanol synthesis reaction circulator power consumption, ethylene glycol per ton can reduce circulator power consumption in oxonation
It is more than 300KW.h/t ethylene glycol, in hydrogenation reaction ethylene glycol per ton can reduce circulator power consumption 100KW.h/t ethylene glycol with
On, methyl alcohol per ton can be reduced more than circulator power consumption 56KW.h/t methyl alcohol in methanol synthesis reaction；
3rd, it is outer flat using outer loading of catalyst tubes of leaking water in coiled pipe pipe, manage, Catalyst packing and the very convenient letter of self-unloading
Victory, ensures that gas flows radially across beds, gas flow direction and water flow direction using outer inflator and interior inflator technology
It is plumbness；Using coiled pipe and point water polo chamber and a spherical cavity interior welds of catchmenting, realization completes snake under the premise of not drawing off catalyst
Pipe leak source is overhauled；
4th, it is main heat-exchanging tube bundle to use coiled pipe, and water-intake pipe is outer flat in pipe, and water is turbulence state in pipe, and gas side water side passes
Hot coefficient is high, and gas flow direction is plumbness with water flow direction, and total heat transfer coefficient heat energy power of moving high is strong, accomplishes catalysis
Agent bed is approximate isothermal bed, is prevented effectively from bed overtemperature, coking (hydrogenation reaction), nitrous acid heating thermal decomposition phenomenon (carbonyl
Change reaction) occur and wax deposition (methanol synthesis reaction), prevent security incident generation；
5th, gas Radial Flow, resistance are low, and loaded catalyst is more, it is strong to move heat energy power, meets ethylene glycol, methanol device big
Typeization needs, 10~300,000 tons of oxonation devices or hydrogenation reactor one of ethylene glycol, and carbonylation/hydrogenation plant is only one
Individual series, can make existing carbonylation/hydrogenation plant floor space reduce by more than 50%, construction investment reduction by more than 50%, operation
Operating cost reduction by more than 40%；900000 tons of methanol devices, one reactor；
6th, it is Natural Circulation to use the waterway circulating between drum and coiled pipe tube bank, effectively prevents existing forced circulation carbonylation
There is oxonation device when having a power failure suddenly in reaction unit and the accident of carbonylation system blast occurs, while prevent existing pressure following
The accidents such as hydrogenation reactor overtemperature coking when having a power failure suddenly in ring hydrogenation reaction device, it is ensured that maximization methanol synthesizer there is
Side reaction thing≤1000PPm.
Brief description of the drawings
Fig. 1 is structural representation of the invention.
Specific embodiment
Embodiments of the invention are elaborated below, the present embodiment is carried out under premised on technical solution of the present invention
Implement, give detailed implementation method and specific operating process, but protection scope of the present invention is not limited to following implementations
Example.
Embodiment 1
As shown in figure 1, the present embodiment include pressure-bearing shell, catalyst framework and heat-exchanging tube bundle, the catalyst framework and
Heat-exchanging tube bundle is separately positioned in pressure-bearing shell；The heat-exchanging tube bundle includes outlet pipe 4, spherical cavity of catchmenting header 7, coiled pipe 11, divides
Water polo chamber header 13 and water inlet pipe 18, the outlet pipe 4 are arranged on the top of pressure-bearing shell, described to catchment the one of spherical cavity header 7
The import of end connection outlet pipe 4, the other end is connected by branch pipe with the outlet of coiled pipe 11, the coiled pipe 11 along pressure-bearing shell axle
To distribution, described point of one end of water polo chamber header 13 connects the import of coiled pipe 11 by branch pipe, other end connection water inlet pipe 18
Outlet, the water inlet pipe 18 is connected to the bottom of pressure-bearing shell.
Maintainer can respectively enter the inside of point water polo chamber header 13 and spherical cavity of catchmenting by water inlet pipe 18 and outlet pipe 4
Inside header 7, completion coiled pipe 11 weld seam maintenance under the premise of catalyst is not drawn off.
Pressure-bearing shell includes upper cover 5, housing 9, support platform 16, low head 17；The upper cover 5 and housing 9 pass through
Flange 8 is connected, and the support platform 16 is arranged on low head 17, and the low head 17 is fixed on the bottom of housing 9.Pressure-bearing shell
Body is not involved in reaction, is primarily subjected to pressure, does not contact high-temperature reacting gas.
Upper cover 5 is provided with thermocouple port 1, delivery port 2 and upper gas port 3, and the outlet pipe 4 is arranged in delivery port 2；Under
End socket 17 is provided with lower gas port 19, water inlet 20 and catalyst self-unloading mouth 21；The water inlet pipe 18 is arranged in water inlet 20.
The catalyst framework includes flat cover 6, outer inflator 10, interior inflator 12, chuck 14 and wireway 15；The flat cover 6
The top of the spherical cavity header 7 that catchments is arranged on, along the axially arranged of housing 9, the interior inflator 12 is arranged outside the outer inflator 10
In inflator 10, the coiled pipe 11 is arranged in the space between outer inflator 10 and interior inflator 12, the outer inflator 10 and housing 9 it
Between there is space, it is described to catchment spherical cavity header 7 and point water polo chamber header 13 is separately positioned on the top and bottom of outer inflator 10, institute
State chuck 14 to be set on point water polo chamber header 13, the chuck 14 is respectively communicated with interior inflator 12 and wireway 15, the air guide
Pipe 15 is connected in lower gas port 19, and described point of water polo chamber header 13 and chuck 14 are supported in support platform 16, the outlet pipe
4th, flat cover 6, spherical cavity of catchmenting header 7, outer inflator 10, coiled pipe 11, interior inflator 12, chuck 14, wireway 15, water inlet pipe 18 are formed
Loading catalyst in space.
The method that the present embodiment carries out hydrogenation reaction using above-mentioned reactor, comprises the following steps：
(11) copper silicon systems catalyst is loaded in catalyst inframe；
(12) leak water from the bottom to top in coiled pipe 11, upper gas port 3 enters reacting gas, and catalysis is passed radially through by outer inflator 10
There is hydrogenation reaction or methanol synthesis reaction to interior inflator 12 in agent bed；
(13) after reacting, the water decalescence in coiled pipe 11, after the hydrogenation or methanol synthesis reaction of catalyst inframe
Heat is removed, and gas is then collected by interior inflator 12, into chuck 14 and the annular space of point water polo chamber header 13, is pooled to wireway
15, heat is then discharged and taken away through lower gas port 19.
Hydrogenation reaction is carried out using the reactor of the present embodiment, CH can be completed3OCOCOCH3O+2H2=HOCH2COOCH3+
CH3OH+QPut、HOCH2COOCH3+2H2=HOCH2CH2OH+CH3OH+QPut、HOCH2CH2OH+H2=CH3CH2OH+H2O+QPut、
HOCH2CH2OH+CH3CH2OH=HOCH2C(CH2CH3)HOH+H2O+QPutEtc. hydrogenation reaction, reaction releases heat by coiled pipe 11
Water absorbs and removes beds heat, and by-product 1.0~2.5MPa saturated vapors.
Embodiment 2
The method that the present embodiment carries out oxonation using described reactor, comprises the following steps：
(21) palladium series catalyst is loaded in catalyst inframe；
(22) leak water from the bottom to top in coiled pipe 11, lower gas port 19 enters reacting gas, into chuck 14 and a point water polo chamber header
13 annular space, beds to outer inflator 10 are passed radially through by interior inflator 12, and oxonation occurs；
(23) after reacting, the water decalescence in coiled pipe 11 removes the heat after the oxonation of catalyst inframe, gas
Body is then collected by outer inflator 10, and heat is then discharged and taken away through upper gas port 3.
Using the reactor of the present embodiment, 2CH can be completed3ONO+2CO=CH3OCOCOCH3O+2NO+QPut、2CH3ONO+
CO=CH3OCOCH3O+2NO+QPut、2CH3ONO=HCHO+CH3OH+2NO+QPutDeng oxonation, reaction releases heat by coiled pipe
Water absorbs and removes beds heat in 11, and by-product 0.08~0.12MPa saturated vapors.
The gas of the present embodiment is moved towards with embodiment 1 conversely, other embodiment and embodiment 1 are identical.
Embodiment 3
The method that the present embodiment carries out methanol synthesis reaction using described reactor, comprises the following steps：
(31) copper-zinc system catalyst is loaded in catalyst inframe；
(32) leak water from the bottom to top in coiled pipe 11, upper gas port 3 enters reacting gas, and catalysis is passed radially through by outer inflator 10
There is H to interior inflator 12 in agent bed2With CO, CO2Generation CH3OH (methyl alcohol) synthetic reaction；
(33) after reacting, the water decalescence in coiled pipe 11 moves the heat after the methanol synthesis reaction of catalyst inframe
Go out, gas is then collected by interior inflator 12, into chuck 14 and the annular space of point water polo chamber header 13, be pooled to wireway 15, then
Heat is discharged and taken away through lower gas port 19.
Using the reactor of the present embodiment, 2H can be completed2+ CO=CH3OH+QPut、3H2+CO2=CH3OH+H2O+QPutEtc. first
Alcohol synthesis reaction, reaction is released heat and absorbs removal beds heat by water in coiled pipe 11, and 2.0~3.8MPa of by-product is full
And steam.
Other embodiment and embodiment 1 are identical.
Presently preferred embodiments of the present invention is the foregoing is only, is not intended to limit the invention, it is all in essence of the invention
Any modification, equivalent and improvement made within god and principle etc., should be included within the scope of the present invention.
Claims (9)
1. the spherical cavity header coil pipe reactor of a kind of water route Natural Circulation, it is characterised in that including pressure-bearing shell, catalyst frame
Body and heat-exchanging tube bundle, the catalyst framework and heat-exchanging tube bundle are separately positioned in pressure-bearing shell；The heat-exchanging tube bundle includes
Water pipe, spherical cavity of catchmenting header, coiled pipe, point water polo chamber header and water inlet pipe, the outlet pipe are arranged on the top of pressure-bearing shell, institute
The one end for stating the spherical cavity header that catchments connects the import of outlet pipe, and the other end is connected by branch pipe with the outlet of coiled pipe, the coiled pipe
It is distributed along the axial direction of pressure-bearing shell, described point of one end of water polo chamber header connects the import of coiled pipe, other end connection by branch pipe
The outlet of water inlet pipe, the water inlet pipe is connected to the bottom of pressure-bearing shell.
2. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 1, it is characterised in that institute
Stating pressure-bearing shell includes upper cover, housing, support platform, low head；The upper cover and housing are connected by flange, the branch
Support platform is arranged on low head, and the low head is fixed on the bottom of housing.
3. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 2, it is characterised in that institute
State upper cover and be provided with thermocouple port, delivery port and upper gas port, the outlet pipe is arranged in delivery port.
4. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 2, it is characterised in that institute
State low head and be provided with lower gas port, water inlet and catalyst self-unloading mouthful；The water inlet pipe is arranged in water inlet.
5. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 4, it is characterised in that institute
Stating catalyst framework includes flat cover, outer inflator, interior inflator, chuck and wireway；The flat cover is arranged on the spherical cavity header that catchments
Top, along the axially arranged of housing, the interior inflator is set in outer inflator the outer inflator, and the coiled pipe is arranged at outer inflator
And in the space between interior inflator, there is space, spherical cavity header and point water polo chamber of catchmenting between the outer inflator and housing
Header is separately positioned on the top and bottom of outer inflator, and the chuck is set on point water polo chamber header, and the chuck connects respectively
Inflator and wireway in logical, the wireway are connected in lower gas port, and described point of water polo chamber header and chuck are supported on support and put down
On platform, what the outlet pipe, flat cover, spherical cavity of catchmenting header, outer inflator, coiled pipe, interior inflator, chuck, wireway, water inlet pipe were formed
Loading catalyst in space.
6. a kind of reactor using as described in any one of Claims 1 to 5 carries out the side of hydrogenation reaction or methanol synthesis reaction
Method.
7. method according to claim 6, it is characterised in that comprise the following steps：
(11) copper silicon systems or copper-zinc system catalyst are loaded in catalyst inframe；
(12) leak water from the bottom to top in coiled pipe, upper gas port enters reacting gas, and beds are passed radially through extremely by outer inflator
, there is hydrogenation reaction or methanol synthesis reaction in interior inflator；
(13) after reacting, the water decalescence in coiled pipe moves the heat after the hydrogenation or methanol synthesis reaction of catalyst inframe
Go out, gas is then collected by interior inflator, into chuck and the annular space of point water polo chamber header, heat is then discharged and taken away through lower gas port
Amount.
8. a kind of method that reactor using as described in any one of Claims 1 to 5 carries out oxonation.
9. method according to claim 8, it is characterised in that comprise the following steps：
(21) palladium series catalyst is loaded in catalyst inframe；
(22) leak water from the bottom to top in coiled pipe, lower gas port enters reacting gas, into chuck and the annular space of point water polo chamber header, pass through
Interior inflator passes radially through beds to outer inflator, and oxonation occurs；
(23) react after, the water decalescence in coiled pipe, by after the oxonation of catalyst inframe heat remove, gas then by
Outer inflator is collected, and heat is then discharged and taken away through upper gas port.
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Application publication date: 20170531 |