CN201135882Y - Axis radial direction low resistance synthesis reactor - Google Patents

Axis radial direction low resistance synthesis reactor Download PDF

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Publication number
CN201135882Y
CN201135882Y CNU200720184534XU CN200720184534U CN201135882Y CN 201135882 Y CN201135882 Y CN 201135882Y CN U200720184534X U CNU200720184534X U CN U200720184534XU CN 200720184534 U CN200720184534 U CN 200720184534U CN 201135882 Y CN201135882 Y CN 201135882Y
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Prior art keywords
gas
pipe
reactor
cover plate
air
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Expired - Fee Related
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CNU200720184534XU
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Chinese (zh)
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沈建冲
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沈建冲
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Abstract

The utility model discloses an axial and radial low resistance synthesis reactor. A radial gas fluid diversion device composed of a gas collector, a fluid director and a gas separator is arranged under the reactor, and the reactor is suitable for the occasion of the chemical product such as the synthesis methyl alcohol. The synthesis reactor has the advantages that the resistance is low, the power consumption is small, the producing quantity is high, the manufacturing cost is low, the operation is convenient, and the accessorial vapor can be produced.

Description

Bearing axial-radius low resistance synthesis reactor
Technical field
The utility model relates to a kind of synthesis reactor, especially has the radially bearing axial-radius low resistance synthesis reactor of guiding device of gas, can be used for the occasion of chemical products such as synthesizing methanol.
Background technology
At present, the cold-tube type holoaxial that domestic and international chemical enterprise generally adopts is to the methanol synthesis reactor of structure, be that logical supercooling tube transmits the heat that produces in the synthetic reaction, thereby reduce the radial and axial temperature difference of reaction bed, but, because the tower diameter of this kind reactor is less, the gas flow process is longer, therefore, the pressure reduction and the resistance of this reactor are bigger, and the power consumption in the production process is higher; In addition, holoaxial generally is provided with heat exchanger to the bottom of medium and small tower diameter reactor, and a part of heat of heat exchanger comes from the high-temperature gas that reclaims out reaction bed, thereby, reduced the temperature of exhaust gas, reduced the callable heat of exhaust gas; Also reduced the useful space in the tower simultaneously, reduced the loadings of catalyst, reduced the output of synthesis gas because of the existence of heat exchanger.
The utility model content
The utility model is at the deficiencies in the prior art, the bearing axial-radius low resistance synthesis reactor that resistance was little, power consumption is low, callable heat is many, output is high, production cost is low when a kind of gas flow was provided.
For realizing above goal of the invention, the utility model by the following technical solutions:
A kind of bearing axial-radius low resistance synthesis reactor, comprise minor flaps 1, large cover 2, cylindrical shell 3, cooler tube bundle 4, support 5, catalyst supporting mechanism 10, gas outlet 12 and air inlet 13, be provided with radially guiding device of gas below support 5, described gas radially guiding device comprises gas collector 7, air deflector 8 and steam separator 9; The cavity that gas collector 7 is made up of upper cover plate 71, gas collecting jar with ground-on cover plate 72, lower cover 73 has air admission hole 721 on the gas collecting jar with ground-on cover plate 72; Air deflector 8 is the cavitys that are interconnected with gas collector 7, has venthole 811 on the guide shell 81 in the air deflector 8; Steam separator 9 is the cavitys around cylindrical shell 3 inboards, has air admission hole 921 on the shunting tube 92 in the steam separator 9, and steam separator 9 bottoms have venthole 931.
As one of technique scheme example preferably, the center line of the air admission hole 921 on the air admission hole 721 on the gas collecting jar with ground-on cover plate 72, the venthole 811 on the guide shell 81, the shunting tube 92 and the radial parallel of reactor.
As another example preferably of technique scheme, upper cover plate 71 and lower cover 73 are tapered, and gas collecting jar with ground-on cover plate 72 is cylindrical, form olivary cavity between upper cover plate 71, lower cover 73 and the gas collecting jar with ground-on cover plate 72.
As another example preferably of technique scheme, the trumpet-shaped cavity that catalyst supporting mechanism 10 is made up of conical plate 101, cylinder 102, end socket 103; Air inlet 13 and central tube 11 are communicated with through pipe 14.
Another example preferably as technique scheme, cooler tube bundle 4 comprises air entraining pipe 41, goes up gas-distributing pipe 42, descending cold pipe 43, up cold pipe 44 and following gas-distributing pipe 45, last gas-distributing pipe 42 is communicated with air entraining pipe 41, descending cold pipe 43, following gas-distributing pipe 45 is communicated with descending cold pipe 43, up cold pipe 44, and the described gas-distributing pipe 42 of going up all is circular straighttubes with following gas-distributing pipe 45.
Another example preferably as technique scheme also has annular cooling tube 6 in the inside of gas collector 7.
The beneficial effects of the utility model are, can reduce the resistance of synthesis reactor significantly, compare to synthesis reactor with holoaxial and can reduce tower resistance 35%-45%; Can reduce power consumption significantly, save the energy; Reaction heat rate of recovery height has increased the output of by-product steam; The catalyst filling coefficient increases, and has improved the production capacity of reactor, reduces production costs; Can also draw off catalyst automatically, reduce the labour intensity when changing catalyst.
Description of drawings
Fig. 1 is the structural representation of the synthesis reactor that independently is provided with of air deflector among the present invention, steam separator;
Fig. 2 is the structural representation of the synthesis reactor that air deflector independently is provided with among the present invention;
Fig. 3 is the structural representation of the synthesis reactor of air deflector among the present invention, steam separator and the binding of catalyst supporting mechanism;
Fig. 4 is the structural representation that has the synthesis reactor of catalyst body dumping mechanism among the present invention.
The specific embodiment
In the embodiment shown in fig. 1, the diameter of axle comprises minor flaps 1, large cover 2, cylindrical shell 3, cooler tube bundle 4, support 5, annular cooling tube 6, gas collector 7, air deflector 8, steam separator 9, catalyst supporting mechanism 10, gas outlet 12 and air inlet 13 to synthesis reactor, can also comprise central tube 11.Minor flaps 1, cylindrical shell 3 is airtight separately by large cover 2, forms that top is divided into collection chamber, the bottom is divided into reative cell.Cooler tube bundle 4 comprises air entraining pipe 41, goes up gas-distributing pipe 42, descending cold pipe 43, up cold pipe 44 and following gas-distributing pipe 45, last gas-distributing pipe 42 is communicated with air entraining pipe 41, descending cold pipe 43, following gas-distributing pipe 45 is communicated with descending cold pipe 43, up cold pipe 44, last gas-distributing pipe 42, following gas-distributing pipe 45 can be circular straighttubes, also can be circular endless tubes; Descending cold pipe 43, up cold pipe 44 can substitute with the cold pipe of U type.Air entraining pipe 41 is by movable sealing between stuffing-box and the large cover 2.The below of cooler tube bundle 4 is provided with support 5, is used to support cooler tube bundle 4.The below of support 5 is provided with radially guiding device of gas, and this guiding device comprises gas collector 7, air deflector 8 and steam separator 9; The cavity that gas collector 7 is made up of upper cover plate 71, gas collecting jar with ground-on cover plate 72, lower cover 73, optimal way is that upper cover plate 71 and lower cover 73 are tapered, gas collecting jar with ground-on cover plate 72 is cylindrical, form olivary cavity between upper cover plate 71, lower cover 73 and the gas collecting jar with ground-on cover plate 72, so that gas flow is smooth and easy, and help the catalyst loading and unloading; Have radial air inlet hole 721 on the gas collecting jar with ground-on cover plate 72; Also has annular cooling tube 6 in the inside of gas collector 7, the quench gas of introducing from the top of reactor, enter in the cavity of gas collector 7 through annular cooling tube 6, join the temperature of regulating the reaction gas in gas collector 7 cavitys with the reaction gas of the cavity that enters into gas collector 7 from radial air inlet hole 721; The cavity that air deflector 8 is made up of guide shell 81, base plate 82 has radially venthole 811 on the guide shell 81; Cavity in air deflector 8 and the gas collector 7 is interconnected; When being provided with central tube 11 in the reactor, gas collector 7, air deflector 8 can be sleeved on the central tube 11; The cavity around cylindrical shell 3 inboards that steam separator 9 is made up of shrouding 91, shunting tube 92, base plate 93 has radial air inlet hole 921 on the shunting tube 92, has venthole 931 on the base plate 93.The center line of the air admission hole 921 on the air admission hole 721 on the gas collecting jar with ground-on cover plate 72, the venthole 811 on the guide shell 81, the shunting tube 92 and the radial parallel of reactor are with guiding reaction gas Radial Flow.Catalyst supporting mechanism 10 is a circular slab, is connected with the lower end of shunting tube 92, in order to support the catalyst layer in the reative cell.Below reactor, be provided with gas outlet 12 and air inlet 13; When reactor was not established central tube 11, air inlet 13 also can be located at the top of reactor.
Unstripped gas enters into collection chamber from air inlet 13, is diverted to gas-distributing pipe 42 through air entraining pipe 41, is redistributed after descending cold pipe 43 flows downward by last gas-distributing pipe 42, and the reaction heat outer with pipe carries out heat exchange, and heating raw gas; Unstripped gas after the heating through gas-distributing pipe 45 shuntings down after up cold pipe 44 bafflings upwards, and with the outer further heat exchange of reaction heat of pipe, and continue heating raw gas, remove the heat that produces in the synthetic reaction with this, and make unstripped gas obtain preheating.When last gas-distributing pipe 42, when gas-distributing pipe 45 is circular straighttube down, owing to descending cold pipe 43, up cold pipe 44 distribute more evenly rationally, make that the isoplanar temperature difference of conversion zone is littler in conversion zone, prolonged the service life of catalyst.Going out unstripped gas behind the up cold pipe 44 enters catalyst layer carry out synthetic reaction under the catalytic action of catalyst.Enter into and be provided with gas radially during the conversion zone of guiding device when synthetic reaction gas leaves the cold leg bed, reaction gas changes Radial Flow into by axial flow, radial air inlet hole 721 on gas collecting jar with ground-on cover plate 72 enters into the cavity of gas collector 7, from top to bottom flows in the cavity of gas collector 7.Owing in the cavity of gas collector 7 and air deflector 8 catalyst is not installed, therefore, reaction gas very enters into the cavity of air deflector 8 glibly, the radially venthole 811 of reaction gas on guide shell 81 enters into catalyst layer again and carries out synthetic reaction, and the radial air inlet hole 921 on shunting tube 92 enters in the steam separator 9,12 goes out reactor by venthole 931 through the gas outlet.Because reaction gas radially under the effect of guiding device, makes reaction gas change the diameter of axle into to flowing by single axial flow at gas, therefore, can reduce the axial pressure difference of conversion zone significantly, thereby reduce the resistance of gas flow in the reactor.Compare to synthesis reactor with holoaxial, can reduce tower resistance 30%-45%, and then can reduce the power consumption of circulator, saves energy significantly.Owing in this reactor heat exchanger is not set, therefore, can effectively improve the packing factor of catalyst, improve the production capacity of reactor, reduce the production cost of unit product.And, can improve the temperature of exhaust gas, reclaim a reaction heat by useless pot, increase the output of by-product steam.
In the embodiment shown in Figure 2, different with Fig. 1 is, steam separator 9 is by the cavity of forming between shrouding 91, shunting tube 92 and the catalyst supporting mechanism 10 around cylindrical shell 3 inboards, and catalyst supporting mechanism 10 is a circular slab, has venthole 931 in the outside of circular slab.
In the embodiment shown in fig. 3, different with Fig. 2 is that air deflector 8 is by the cavity of forming between guide shell 81 and the catalyst supporting mechanism 10.
In the embodiment shown in fig. 4, different with Fig. 1 is the trumpet-shaped cavity that catalyst supporting mechanism 10 is made up of conical plate 101, cylinder 102, end socket 103.When reactor was worked, this cavity supported catalyst layer; When needs repair apparatus or replacing catalyst, by opening end socket 103 catalyst is drawn off automatically from reactor, the labour intensity when reducing the replacing catalyst with this.Air inlet 13 and central tube 11 are communicated with through pipe 14.Unstripped gas enters through air inlet 13, enters central tube 11 behind pipe 14.
In the pure system of connection, use this reactor, 4.0 cubes of filling C207 catalyst for methanol, inlet tower gas composition (%) is: H 274.0, CO 3.8, CO 20.4, N 220.3, CH 4Deng 1.5, inlet tower gas pressure 12.2Mpa goes into 215 ℃ of bed temperatures, exhaust gas pressure 11.9Mpa, 248 ℃ of exhaust gas temperature, 1.6 tons of hour product alcohol, 850 kilograms of by-product 0.5Mpa steam.

Claims (6)

1, a kind of bearing axial-radius low resistance synthesis reactor, comprise minor flaps (1), large cover (2), cylindrical shell (3), cooler tube bundle (4), support (5), catalyst supporting mechanism (10), gas outlet (12) and air inlet (13), it is characterized in that being provided with radially guiding device of gas in the below of support (5), described gas radially guiding device comprises gas collector (7), air deflector (8) and steam separator (9); The cavity that gas collector (7) is made up of upper cover plate (71), gas collecting jar with ground-on cover plate (72), lower cover (73) has air admission hole (721) on the gas collecting jar with ground-on cover plate (72); Air deflector (8) is the cavity that is interconnected with gas collector (7), has venthole (811) on the guide shell (81) in the air deflector (8); Steam separator (9) is around the inboard cavity of cylindrical shell (3), has air admission hole (921) on the shunting tube (92) in the steam separator (9), and steam separator (9) bottom has venthole (931).
2, reactor according to claim 1 is characterized in that the air admission hole (721), the venthole (811) on the guide shell (81) on the gas collecting jar with ground-on cover plate (72), air admission hole (921 the center line and the radial parallel of reactor on the shunting tube (92).
3, reactor according to claim 1 is characterized in that upper cover plate (71) and lower cover (73) are all tapered, and gas collecting jar with ground-on cover plate (72) is cylindrical, forms olivary cavity between upper cover plate (71), lower cover (73) and the gas collecting jar with ground-on cover plate (72).
4, reactor according to claim 1 is characterized in that the trumpet-shaped cavity that catalyst supporting mechanism (10) is made up of conical plate (101), cylinder (102), end socket (103); Air inlet (13) and central tube (11) are communicated with through pipe (14).
5,, it is characterized in that also having annular cooling tube (6) in the inside of gas collector (7) according to each described reactor in the claim 1 to 4.
6, reactor according to claim 5, it is characterized in that cooler tube bundle (4) comprises air entraining pipe (41), goes up gas-distributing pipe (42), descending cold pipe (43), up cold pipe (44) and following gas-distributing pipe (45), last gas-distributing pipe (42) is communicated with air entraining pipe (41), descending cold pipe (43), following gas-distributing pipe (45) is communicated with descending cold pipe (43), up cold pipe (44), and described upward gas-distributing pipe (42) and following gas-distributing pipe (45) all are circular straighttubes.
CNU200720184534XU 2007-10-29 2007-10-29 Axis radial direction low resistance synthesis reactor Expired - Fee Related CN201135882Y (en)

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CNU200720184534XU CN201135882Y (en) 2007-10-29 2007-10-29 Axis radial direction low resistance synthesis reactor

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103657532A (en) * 2013-12-13 2014-03-26 衢州昀睿工业设计有限公司 Self-circulation chemical synthesizer
CN103691368A (en) * 2013-12-17 2014-04-02 衢州昀睿工业设计有限公司 One-way compression type self-circulation chemical synthesis reactor
CN103691367A (en) * 2013-12-15 2014-04-02 衢州昀睿工业设计有限公司 Equal-pressure self-circulation chemical synthesizer
CN103706308A (en) * 2013-12-16 2014-04-09 衢州昀睿工业设计有限公司 Self-circulation chemical synthesis reactor
CN108786663A (en) * 2017-05-02 2018-11-13 中国石化工程建设有限公司 A kind of catalyst bed reactor that can be replaced online

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103657532A (en) * 2013-12-13 2014-03-26 衢州昀睿工业设计有限公司 Self-circulation chemical synthesizer
CN103691367A (en) * 2013-12-15 2014-04-02 衢州昀睿工业设计有限公司 Equal-pressure self-circulation chemical synthesizer
CN103691367B (en) * 2013-12-15 2015-06-10 衢州昀睿工业设计有限公司 Equal-pressure self-circulation chemical synthesizer
CN103706308A (en) * 2013-12-16 2014-04-09 衢州昀睿工业设计有限公司 Self-circulation chemical synthesis reactor
CN103706308B (en) * 2013-12-16 2015-08-26 衢州昀睿工业设计有限公司 A kind of self-loopa combination reaction device
CN103691368A (en) * 2013-12-17 2014-04-02 衢州昀睿工业设计有限公司 One-way compression type self-circulation chemical synthesis reactor
CN103691368B (en) * 2013-12-17 2015-06-10 衢州昀睿工业设计有限公司 One-way compression type self-circulation chemical synthesis reactor
CN108786663A (en) * 2017-05-02 2018-11-13 中国石化工程建设有限公司 A kind of catalyst bed reactor that can be replaced online

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Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
EE01 Entry into force of recordation of patent licensing contract

Assignee: Hangzhou Kuaikai High-Efficiency Energy-Saving New Techn Co., Ltd.

Assignor: Shen Jianchong

Contract fulfillment period: 2008.9.30 to 2015.9.29

Contract record no.: 2008330002501

Denomination of utility model: Axis radial direction low resistance synthesis reactor

Granted publication date: 20081022

License type: Exclusive license

Record date: 20081201

LIC Patent licence contract for exploitation submitted for record

Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2008.9.30 TO 2015.9.29; CHANGE OF CONTRACT

Name of requester: HANGZHOU KUAIKAI ENERGY EFFICIENT NEW TECHNOLOGIES

Effective date: 20081201

C17 Cessation of patent right
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20081022

Termination date: 20121029