CN106629775A - Multitube-type ultra-low-pressure isothermal ammonia converter - Google Patents
Multitube-type ultra-low-pressure isothermal ammonia converter Download PDFInfo
- Publication number
- CN106629775A CN106629775A CN201710035164.1A CN201710035164A CN106629775A CN 106629775 A CN106629775 A CN 106629775A CN 201710035164 A CN201710035164 A CN 201710035164A CN 106629775 A CN106629775 A CN 106629775A
- Authority
- CN
- China
- Prior art keywords
- tube
- pipe
- shell
- inner core
- pressure isothermal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 37
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 28
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 26
- 238000009826 distribution Methods 0.000 claims abstract description 23
- 238000001704 evaporation Methods 0.000 claims abstract description 10
- 239000006185 dispersion Substances 0.000 claims description 34
- 230000035939 shock Effects 0.000 claims description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 238000006392 deoxygenation reaction Methods 0.000 claims description 15
- 230000008020 evaporation Effects 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 230000001174 ascending effect Effects 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 37
- 239000000126 substance Substances 0.000 description 7
- 239000003054 catalyst Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 241000486406 Trachea Species 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 210000003437 trachea Anatomy 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
- C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
- C01C1/0417—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
- C01C1/0441—Reactors with the catalyst arranged in tubes
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention relates to an ammonia converter, and especially relates to a multitube-type ultra-low-pressure isothermal ammonia converter. The multitube-type ultra-low-pressure isothermal ammonia converter comprises a converter body composed of an inner tube and an outer tube; and the multitube-type ultra-low-pressure isothermal ammonia converter is characterized in that a main steam pipe, a cold-shock air pipe and a material filling pipe are connected to the inner top of the inner tube; multitube-type deoxidizing and water-evaporating tubes are connected to the bottom of the main steam pipe via multiple steam distribution tubes; an air ascending pipe is arranged in the inner tube at the center and around; and a heat exchange pipe is arranged under the air ascending pipe. The multitube-type ultra-low-pressure isothermal ammonia converter has the following beneficial effects: overall heat exchange is continuously performed on the synthesized gas in the converter, so that the pressure required for the synthesis reaction is greatly reduced; moreover, the temperature at the upper part and the lower part of the converter are maintained identical, so that the conversion rate of the ammonia synthesis is improved. The multitube-type ultra-low-pressure isothermal ammonia converter is simple in processing, economical in cost, reduced in energy consumption, safe, and reliable.
Description
（One）Technical field
The present invention relates to a kind of ammonia convertor, more particularly to a kind of shell and tube ultralow pressure isothermal ammonia convertor.
（Two）Background technology
Synthesis ammonia refers to the ammonia being directly synthesized in the presence of the catalyst at elevated temperature and pressure by nitrogen and hydrogen, is a kind of basic inorganic chemical industry
Flow process.In modern chemical industry, ammonia is the primary raw material of chemical fertilizer industry and basic organic chemical industry, occupies important in national economy
Status, wherein there are about 80% ammonia for producing chemical fertilizer, 20% is the raw material of other chemical products.Ammonia convertor is referred to as synthesis
The heart of ammonia factory, it is one of Chief equipment in whole synthesis ammonia plant production process.
In chemical industry, the ammonia conversion ratio of conventional synthesis tower is relatively low（10%～12%）, synthesis pressure is higher（22.0 MPa
～32.0MPa）, energy consumption of unit product is very high.Later because purification techniques improvement, gas componant improvement, foreign gas content are by 1%
～5% drops to 10ppm～50ppm, and the structure of synthetic tower also there occurs change, increase heat exchange area between catalyst section, reduces
Synthesis mean temperature, therefore, the ammonia conversion ratio of synthetic tower is improved（15%～18%）, synthesis pressure reduction（12.0 MPa～
15.0MPa）, energy consumption of unit product is decreased obviously.But, synthesis pressure still above 10MPa, more than 10 Mpa for synthesis
For tower, difficulty of processing is big, high processing costs, operating risk are high, and operation energy consumption is also high.
（Three）The content of the invention
The present invention is in order to make up the deficiencies in the prior art, there is provided one kind processes simple, cost-effective, reducing energy consumption, safety can
By the shell and tube ultralow pressure isothermal ammonia convertor of, ammonia high conversion rate.
The present invention is achieved through the following technical solutions：
A kind of shell and tube ultralow pressure isothermal ammonia convertor, including the tower body being made up of inner core and outer tube, is characterized in that：The inner core
Inner top is connected with main steam range, cold shock tracheae and is filled with expects pipe, and main steam range bottom is arranged by the connection of some distribution of steam pipes
Tubular type deaerated water evaporation tube, is provided with the riser positioned at center and surrounding in inner core, riser lower section is provided with heat exchanger tube.
The cold shock tracheae bottom connects some cold shock gas distributor pipes, and cold shock gas distributor pipe is stretched into dispersion pipe, dispersion pipe
Top is provided with gas dispersion plate, and dispersion pipe middle and lower part is connected with dispersion arm, on dispersion pipe and dispersion arm dispersion is offered
Hole, is provided with some baffle plates inside dispersion pipe.
Deflection plate is provided between the heat exchanger tube, heat exchanger tube top is provided with upper perforated plate, and bottom is provided with lower perforated plate.
The inner core top is provided with gas distribution grid, and gas distribution holes are offered on gas distribution grid.
Water conservancy diversion heavy burden cylinder is installed, if being uniformly provided with dry temperature sensor in inner core on the upper perforated plate.
The shell and tube deaerated water evaporation bottom of the tube connects deoxygenation waterpipe by deoxygenation water distribution, under deoxygenation waterpipe
Portion is U-shaped shape.
The inner core centre bottom is provided with lets out loading pipe, lets out loading pipe top and is connected with circular cone end socket, circular cone end socket top
It is connected with inner core inwall, lets out filler bottom of the tube and be provided with and let out feeding port.
The outer tube top is provided with lid, and outer tube upper side offers synthesis gas entrance, and outer tube bottom side offers
Syngas outlet.
The inner core bottom is provided with inner core low head, and outer tube bottom is provided with outer tube low head.
The temperature sensor top is connected with temperature sensor interface, and cold shock tracheae top is connected with cold shock gas interface,
It is filled with expects pipe top and is connected with the filled mouth of pipe, main steam range top is connected with main steam range interface.
The invention has the beneficial effects as follows：Make that synthesis gas is continual in tower to carry out overall heat exchange, substantially reduce synthesis
Pressure needed for reaction, and make upper and lower temperature in tower unanimously, improve the conversion ratio of ammonia synthesis, processing is simple, cost-effective, drop
Low energy consumption, it is safe and reliable.
（Four）Description of the drawings
Below in conjunction with the accompanying drawings the present invention is further illustrated.
Accompanying drawing 1 is main view shaft section structural representation of the invention；
Accompanying drawing 2 is side-looking shaft section structural representation of the invention；
Accompanying drawing 3 is the A-A sectional views of accompanying drawing 1；
Accompanying drawing 4 is the B-B sectional views of accompanying drawing 1；
Accompanying drawing 5 is the D-D sectional views of accompanying drawing 1；
Accompanying drawing 6 is the E-E sectional views of accompanying drawing 1；
Accompanying drawing 7 is the F-F sectional views of accompanying drawing 1；
Accompanying drawing 8 is the G-G sectional views of accompanying drawing 1；
Accompanying drawing 9 is the H-H sectional views of accompanying drawing 1；
Accompanying drawing 10 is the J-J sectional views of accompanying drawing 1；
Accompanying drawing 11 is the C-C sectional views of accompanying drawing 2；
Accompanying drawing 12 is the K-K sectional views of accompanying drawing 2；
Accompanying drawing 13 is the L-L sectional views of accompanying drawing 2；
Accompanying drawing 14 is cold shock air pipe structure schematic diagram of the invention；
In figure, 1 inner core, 2 outer tube, 3 tower bodies, 4 main steam ranges, 5 cold shock tracheaes, 6 are filled with expects pipe, 7 distribution of steam pipes, 8 shell and tubes
Deaerated water evaporation tube, 9 riseies, 10 heat exchanger tubes, 11 cold shock gas distributor pipes, 12 dispersion pipes, 13 gas dispersion plates, 14 dispersions
Pipe, 15 dispersion holes, 16 baffle plates, 17 deflection plates, 18 upper perforated plates, 19 lower perforated plates, 20 gas distribution grids, 21 gas distribution holes, 22 lead
Stream heavy burden cylinder, 23 temperature sensors, 24 deoxygenation water distributions, 25 deoxygenation waterpipes, 26 let out loading pipe, 27 circular cone end sockets, and 28 let out
Feeding port, covers, 30 synthesis gas entrances, 31 syngas outlets, 32 inner core low heads, 33 outer tube low heads, 34 TEMPs on 29
Device interface, 35 cold shock gas interfaces, the 36 filled mouths of pipe, 37 main steam range interfaces.
（Five）Specific embodiment
Accompanying drawing is a kind of specific embodiment of the present invention.The embodiment includes the tower body 3 being made up of inner core 1 and outer tube 2, inner core 1
Inner top is connected with main steam range 4, cold shock tracheae 5 and is filled with expects pipe 6, and the bottom of main steam range 4 is connected by some distribution of steam pipes 7
Shell and tube deaerated water evaporation tube 8 is connect, the riser 9 positioned at center and surrounding is provided with inner core 1, the lower section of riser 9 is provided with heat exchange
Pipe 10.The bottom of cold shock tracheae 5 connects some cold shock gas distributor pipes 11, and cold shock gas distributor pipe 11 is stretched into dispersion pipe 12, dispersion pipe
12 tops are provided with gas dispersion plate 13, and the middle and lower part of dispersion pipe 12 is connected with dispersion arm 14, dispersion pipe 12 and dispersion arm 14
On offer dispersion hole 15, some baffle plates 16 are provided with inside dispersion pipe 12.Deflection plate 17, heat exchanger tube 10 are provided between heat exchanger tube 10
Top is provided with upper perforated plate 18, and bottom is provided with lower perforated plate 19.The top of inner core 1 is provided with gas distribution grid 20, gas distribution grid 20
On offer gas distribution holes 21.It is provided with upper perforated plate 18 in water conservancy diversion heavy burden cylinder 22, inner core 1 and is uniformly provided with some TEMPs
Device 23.The bottom of shell and tube deaerated water evaporation tube 8 connects deoxygenation waterpipe 25 by deoxygenation water distribution 24, under deoxygenation waterpipe 25
Portion is U-shaped shape.The centre bottom of inner core 1 is provided with lets out loading pipe 26, lets out the top of loading pipe 26 and is connected with circular cone end socket 27, circular cone envelope
27 tops are connected with the inwall of inner core 1, let out the bottom of loading pipe 26 and are provided with and let out feeding port 28.The top of outer tube 2 is provided with lid 29, outward
2 upper sides of cylinder offer synthesis gas entrance 30, and the bottom side of outer tube 2 offers syngas outlet 31.In the bottom of inner core 1 is provided with
Cylinder low head 32, the bottom of outer tube 2 is provided with outer tube low head 33.The top of temperature sensor 23 is connected with temperature sensor interface 34,
The top of cold shock tracheae 5 is connected with cold shock gas interface 35, is filled with the top of expects pipe 6 and is connected with the filled mouth of pipe 36, the top of main steam range 4
It is connected with main steam range interface 37.
Using a kind of shell and tube ultralow pressure isothermal ammonia convertor of the present invention, N2、H2, the synthesis gas such as inert gas is from outer tube 2
Synthesis gas entrance 30 enter, the gap between inner core 1 and outer tube 2 always downwards, enters interior by the through hole of the bottom of inner core 1
Rise in cylinder 1, preheated through heat exchanger tube 10, due to the effect of deflection plate 17, the S-type rising of synthesis gas increases heat exchange
Efficiency.Then, synthesis gas rises to always the top of tower body 3 into riser 9, and in the case where upper lid 29 is acted on, synthesis gas passes through gas
The gas distribution holes 21 of distribution grid 20 run downwards, now touch from the catalyst for being filled with the feeding of expects pipe 6, make N2And H2Synthesis
Ammonia, heat release in building-up process, heat makes the deaerated water in shell and tube deaerated water evaporation tube 8 flash to steam and enters main steam range
4, so as to complete to be exchanged heat in tower, make upper and lower temperature in tower equal, improve the conversion ratio of synthetic reaction；Additionally, passing through TEMP
Temperature in 23 moment of device monitoring tower, can simultaneously make cold shock gas pass sequentially through cold shock tracheae 5, cold shock gas distributor pipe 11 even into tower
Inner plane, and then discharged by dispersion hole 15 even into vertical direction in tower by dispersion pipe 12, dispersion arm 14, due to
More down temperature is lower, thus baffle plate 16 can suitable control cold shock gas enter lower section amount.Produce when the gas of synthesis runs downwards
The larger thrust of life, water conservancy diversion heavy burden cylinder 22 not only can play a part of to carry out synthesis gas water conservancy diversion, and can give upper column
The catalyst of body 3 necessarily bears a heavy burden support, prevents from damaging tower body 3.Deoxygenation water distribution can be passed through after deaerated water certain hour
24 enter deoxygenation waterpipe 25, and the swell increment of deaerated water is different with the shell of tower body 3, and then discharge, the U of the bottom of deoxygenation waterpipe 25
Type is curved to eliminate swelling stress.Catalyst positioned at the gap of shell and tube deaerated water evaporation tube 8 can enter in the case where circular cone end socket 27 is acted on
Enter to let out loading pipe 26, and then discharge from feeding port 28 is let out.The ammonia of synthesis is discharged from syngas outlet 31.
Claims (10)
1. a kind of shell and tube ultralow pressure isothermal ammonia convertor, including by inner core（1）And outer tube（2）The tower body of composition（3）, its feature
It is：The inner core（1）Inner top is connected with main steam range（4）, cold shock tracheae（5）Be filled with expects pipe（6）, main steam range（4）Bottom
Portion is by some distribution of steam pipes（7）Connection shell and tube deaerated water evaporation tube（8）, inner core（1）In be provided with positioned at center and surrounding
Riser（9）, riser（9）Lower section is provided with heat exchanger tube（10）.
2. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 1, is characterized in that：The cold shock tracheae
（5）Bottom connects some cold shock gas distributor pipes（11）, cold shock gas distributor pipe（11）Stretch into dispersion pipe（12）It is interior, dispersion pipe（12）On
Portion is provided with gas dispersion plate（13）, dispersion pipe（12）Middle and lower part is connected with dispersion arm（14）, dispersion pipe（12）And dispersion
Pipe（14）On offer dispersion hole（15）, dispersion pipe（12）Inside is provided with some baffle plates（16）.
3. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 1, is characterized in that：The heat exchanger tube（10）
Between be provided with deflection plate（17）, heat exchanger tube（10）Top is provided with upper perforated plate（18）, bottom is provided with lower perforated plate（19）.
4. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 1, is characterized in that：The inner core（1）Top
Portion is provided with gas distribution grid（20）, gas distribution grid（20）On offer gas distribution holes（21）.
5. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 3, is characterized in that：The upper perforated plate（18）
On water conservancy diversion heavy burden cylinder is installed（22）, inner core（1）If being inside uniformly provided with dry temperature sensor（23）.
6. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 1, is characterized in that：The shell and tube deoxygenation
Water evaporation pipe（8）Bottom passes through deoxygenation water distribution（24）Connection deoxygenation waterpipe（25）, deoxygenation waterpipe（25）Bottom is U-shaped
Shape.
7. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 1, is characterized in that：The inner core（1）In
Heart bottom is provided with lets out loading pipe（26）, let out loading pipe（26）Top is connected with circular cone end socket（27）, circular cone end socket（27）Top with
Inner core（1）Inwall is connected, and lets out loading pipe（26）Bottom is provided with lets out feeding port（28）.
8. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 1, is characterized in that：The outer tube（2）Top
Portion is provided with lid（29）, outer tube（2）Upper side offers synthesis gas entrance（30）, outer tube（2）Bottom side offers synthesis
Gas is exported（31）.
9. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 1, is characterized in that：The inner core（1）Bottom
Portion is provided with inner core low head（32）, outer tube（2）Bottom is provided with outer tube low head（33）.
10. a kind of shell and tube ultralow pressure isothermal ammonia convertor according to claim 5, is characterized in that：The TEMP
Device（23）Top is connected with temperature sensor interface（34）, cold shock tracheae（5）Top is connected with cold shock gas interface（35）, it is filled
Pipe（6）Top is connected with the filled mouth of pipe（36）, main steam range（4）Top is connected with main steam range interface（37）.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710035164.1A CN106629775B (en) | 2017-01-18 | 2017-01-18 | tube array type ultra-low pressure isothermal ammonia synthesis tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710035164.1A CN106629775B (en) | 2017-01-18 | 2017-01-18 | tube array type ultra-low pressure isothermal ammonia synthesis tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106629775A true CN106629775A (en) | 2017-05-10 |
| CN106629775B CN106629775B (en) | 2019-12-06 |
Family
ID=58840682
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710035164.1A Expired - Fee Related CN106629775B (en) | 2017-01-18 | 2017-01-18 | tube array type ultra-low pressure isothermal ammonia synthesis tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106629775B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1060636A (en) * | 1991-12-03 | 1992-04-29 | 中国石油化工总公司 | Two-section radial parallel heat exchanging type ammonia synthetic tower |
| EP0994072A1 (en) * | 1998-10-12 | 2000-04-19 | Kellogg Brown & Root, Inc. | Isothermal ammonia converter |
| CN2477267Y (en) * | 2000-11-25 | 2002-02-20 | 陈运根 | Isothermal efficiency self-discharging carbinol synthetic tower inner element |
| CN101554572A (en) * | 2009-05-15 | 2009-10-14 | 新奥新能(北京)科技有限公司 | Methane synthesis reactor |
| CN203550701U (en) * | 2013-11-21 | 2014-04-16 | 兰州兰洛炼化设备有限公司 | Overlapped type spiral plate heat exchanger |
-
2017
- 2017-01-18 CN CN201710035164.1A patent/CN106629775B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1060636A (en) * | 1991-12-03 | 1992-04-29 | 中国石油化工总公司 | Two-section radial parallel heat exchanging type ammonia synthetic tower |
| EP0994072A1 (en) * | 1998-10-12 | 2000-04-19 | Kellogg Brown & Root, Inc. | Isothermal ammonia converter |
| CN2477267Y (en) * | 2000-11-25 | 2002-02-20 | 陈运根 | Isothermal efficiency self-discharging carbinol synthetic tower inner element |
| CN101554572A (en) * | 2009-05-15 | 2009-10-14 | 新奥新能(北京)科技有限公司 | Methane synthesis reactor |
| CN203550701U (en) * | 2013-11-21 | 2014-04-16 | 兰州兰洛炼化设备有限公司 | Overlapped type spiral plate heat exchanger |
Non-Patent Citations (3)
| Title |
|---|
| 谭世语等: "《化学工艺学》", 31 August 2014, 重庆大学出版社 * |
| 陈听宽: "《节能原理与技术》", 31 October 1988, 北京：机械工业出版社 * |
| 黄艳琴，张继昌主编: "《化工工艺学》", 28 February 2012 * |
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| CN106629775B (en) | 2019-12-06 |
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