CN1067656C - Anti-corrosive method and apparatus by heat exchange of saturated gas with changing gas - Google Patents
Anti-corrosive method and apparatus by heat exchange of saturated gas with changing gas Download PDFInfo
- Publication number
- CN1067656C CN1067656C CN95112522A CN95112522A CN1067656C CN 1067656 C CN1067656 C CN 1067656C CN 95112522 A CN95112522 A CN 95112522A CN 95112522 A CN95112522 A CN 95112522A CN 1067656 C CN1067656 C CN 1067656C
- Authority
- CN
- China
- Prior art keywords
- gas
- heat exchange
- coal gas
- conversion
- heat exchanger
- 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.)
- Expired - Lifetime
Links
Images
Landscapes
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The present invention relates to a method for the corrosion prevention of saturated coal gas and conversion gas in heat exchange and a device. Parallel flow heat exchange is carried out to partial conversion gas and low temperature saturated coal gas, the temperature of saturated coal gas is rapidly raised, coal gas is heated into wet coal gas far away from a dew point, dew point corrosion is avoided, counter flow heat exchange is carried out to the other partial conversion gas and the wet coal gas with raised temperature, and the wet coal gas is heated to technically required temperature and then enters a conversion furnace. The devices used by the heat exchange method are a parallel flow multitubular heat exchanger and a counter flow multitubular heat exchanger or a large multitubular heat exchanger and a small multitubular heat exchanger. The method has the advantages of good utilization of the heat quantity of one third of conversion gas originally moved to a water heater, prevention of dew point corrosion, simple device structure, large heat exchange area and device cost saving.
Description
The invention relates to the anti-corrosion method and the heat exchanger device of saturated coal gas of synthesis ammonia plant conversion section and the heat exchange of conversion gas.
In the synthesis ammonia plant conversion section, the coal gas that is come out by saturator is water-vapo(u)r saturation coal gas, this gas can produce serious dew point corrosion to heat exchanger device, makes main heat exchanger leak, and coal gas seals in conversion gas, to Co-Mo is that transformation catalyst harm is serious, cause work-ing life very short, elder half a year, weak point person tens days, need often to change heat exchanger, ammonia synthesis production factory causes very big waste.The heat exchanger position of easy corrosion leakage is near the saturated gas entry of the heat exchanger place that is in the dew point, for the temperature that improves is herein avoided dew point corrosion, a kind of preheating bubble-cap heat exchanger commonly used, this kind heat exchanger is cover on tubulation heat exchanger outer cover, saturated coal gas is introduced into bubble-cap from the bubble-cap bottom, and enter high temperature shift gas between the tubulation pipe heats saturated coal gas by the tubular heat exchange cylindrical shell and is the above wet gas of dew point from the bottom, carry out going out by the heat exchanger bottom after the heat exchange with conversion gas from top to bottom in the tubulation pipe by bubble-cap top then, enter shift converter.With the same end of high temperature shift gas, carry out heat exchange earlier in short, improve the wet gas temperature rapidly, break away from dew point, obtain anticorrosion ability with the low temperature wet gas at preheating bubble-cap heat exchanger.The advantage of this method and apparatus is that device structure is simple, and it is convenient to install, overhaul, and is easier to clean; Shortcoming is that the bubble-cap size is big, and expense is higher; Only inner cylindrical shell is passed to the low temperature wet gas with conversion gas heat, and heat transfer area is little, and the wet gas temperature raising is slow, and not enough to low temperature wet gas heating, corrosion location wet gas temperature is not high, and is nearer from dew-point temperature, corrode byer force, and the inner barrel dead angle is located still perishable.
The carbon monodixe conversion reaction is thermopositive reaction, with conversion gas wet gas is heated to the processing requirement temperature and needs 2/3 conversion gas heat, and 1/3 unnecessary conversion gas heat moves to water heater by the temperature adjustment by-pass with heat at present, does not utilize well.
The objective of the invention is to overcome the deficiency of above-mentioned saturated coal gas and conversion gas heat change method and preheating bubble-cap heat exchanger, a kind of saturated coal gas and conversion gas heat exchange anti-corrosion method and equipment are provided.This method can be utilized 1/3 conversion gas heat better, avoids dew point corrosion, and the structure of heat exchanging apparatus is equally simple with general heat exchanger, install, maintenance is convenient, cleaning easily, and cost is lower than preheating bubble-cap heat exchanger, and heat interchanging area is big, no dead angle, evenly, corrosion is little, the life-span is long.
The technical scheme that realizes above-mentioned purpose is with a part of conversion gas and the saturated coal gas of low temperature and flows heat exchange, improve saturated gas temperature rapidly, make saturated coal gas be heated into unsaturation wet gas away from dew point, avoid dew point corrosion, wet gas counterflow heat exchange with after another part conversion gas and the temperature raising is heated to the processing requirement temperature with wet gas.
The present invention is with 1/3 conversion gas and the saturated coal gas of low temperature and flow heat exchange, improves the wet gas temperature rapidly, avoids dew point corrosion, and with the wet gas counterflow heat exchange of 2/3 conversion gas after with temperature raising, wet gas further is heated to the processing requirement temperature.
Also designed for achieving the above object and the adverse current tubular heat exchanger, this heat exchanger is the same with general tubular heat exchange, form by cylindrical shell, tubulation, tube sheet and traverse baffle, tubulation two is fixed on and is installed in the cylindrical shell on the tube sheet, the fluid (being heated saturated coal gas) at the cylindrical shell two in the tubulation pipe is imported and exported and is communicated, traverse baffle is partitioned into the baffling passage with pipe, there is the import and export of heating fluid (conversion gas) at baffling passage two on cylindrical shell, be characterized in that heating fluid (conversion gas) has major and minor two imports, an outlet; The major-minor import is respectively at cylindrical shell two, outlet is close secondary import in the cylindrical shell middle part, saturated coal gas becomes and flow structure to the outlet tube lane from secondary import from import to the outlet pipe interior passageway with conversion gas, be this heat exchanger and stream section, become counterflow configuration with the tube lane of conversion gas from main import to outlet, be this heat exchanger adverse current section, and stream section 2 traverse baffles are arranged, and the heat exchange area of stream section accounts for 1/5 of the total heat exchange area of this heat exchanger, and adverse current section heat exchange area accounts for 4/5 of the total heat exchange area of this heat exchanger.
For achieving the above object, heat exchanger also can be designed to the primary and secondary heat exchanger.Change number of times for reducing big heat exchanger, before big heat exchanger, establish little heat exchanger, adopt conversion gas and saturated coal gas and stream to descend heat exchange by little heat exchanger the unnecessary heat of conversion gas (1/3 conversion gas heat), the rapid temperature raising of saturated coal gas to away from dew-point temperature, is gone into big heat exchanger and the conversion circulation of vital energy in the wrong direction then and flowed heat exchange and be warmed to processing requirement and remove shift converter.
Advantage of the present invention is: 1, will move to water heater to 1/3 conversion gas heat by the temperature adjustment by-pass originally, and change into and be used for improving saturated gas temperature rapidly, and make wet gas away from dew-point temperature, and greatly reduce the corrosion to equipment.And the heat exchange of stream section can replace the temperature adjustment by-pass to regulate shift converter inlet gas temperature, saved the temperature adjustment by-pass of former obstructed over-heat-exchanger.2, heat converter structure and preheating bubble-cap heat exchanger are simple equally, maintenance are installed conveniently, cleaning easily, and cost is but than preheating bubble-cap heat exchanger low 1/3.Heat exchange area is big.3, directly improve gas temperature by tubulation and tube sheet, no dead angle, the heat exchange uniform high-efficiency can be passed to heat saturated coal gas rapidly.
Embodiments of the invention provide with accompanying drawing.
Fig. 1 is the technology and equipment (and the adverse current tubular heat exchanger) structure iron of the embodiment of the invention 1.
Fig. 2 is the embodiment of the invention 2 technologies and equipment diagrammatic sketch.
Fig. 1 middle cylinder body 1, tubulation 2, tube sheet 3, traverse baffle 4 is formed and the adverse current tubular heat exchanger, there is the saturated gas inlet 5 of low temperature cylindrical shell 1 upper end, there is the wet gas outlet 6 after the heating lower end, coal gas is walked in the tubulation pipe, the secondary import 8 of high temperature shift gas is arranged at cylindrical shell 1 top, high temperature shift gas master import 7 is arranged at the bottom, there is conversion gas outlet 9 at the middle part, conversion is made leave with rage between the tubulation pipe, to 9 of outlets 2 traverse baffles 4 are arranged from the secondary import 8 of conversion gas, the tubulation pipe is partitioned into the passage that flows to and flow with coal gas, this section is this heat exchanger and stream section, the tubulation pipe is partitioned into coal gas flows to into counter-flowing path to 9 traverse baffles 4 of outlet from conversion gas master import 7, this section is this heat exchanger adverse current section.And stream section heat exchange area accounts for 1/5 of total heat exchange area.
A part (1/3) high temperature shift gas is gone into from secondary import 8; with the saturated coal gas of low temperature in the tubulation pipe and flow heat exchange; go out from exporting 9; the saturated coal gas of low temperature is heated rapidly; make warm coal gas away from dew point; tubulation exempts from dew point corrosion in the downward 1 meter scope of protection low temperature wet gas tube sheet; another part (2/3) high temperature shift gas is gone into from hot posture device bottom conversion gas master import 7; flowing upward to outlet 9 between the tubulation pipe goes out; with the wet gas counterflow heat exchange; remove shift converter after wet gas further is heated to the processing requirement temperature, the low temperature shift gas after the heat exchange goes down operation.
The conversion tracheae line that connects the secondary import 8 of conversion gas of this heat exchanger plays the effect of technology temperature adjustment by-pass, saves the anhydrate temperature adjustment by-pass of well heater of original shift converter outlet conversion gas.
Anhui fertilizer plant adopts of the present invention and adverse current tubular heat exchanger, does not still leak with existing more than 2 years, and former tubulation heat exchanger can only use just to be needed to change half a year, and using preheating bubble-cap heat exchanger instead also can only be with 1 year.
Two tubulation heat exchangers of size are adopted in saturated coal gas and the heat exchange of conversion gas among Fig. 2.10 is little heat exchanger (pre-etching heat exchanger), 11 is big heat exchanger (main heat exchanger), the saturated coal gas of low temperature enters from little heat exchanger upper inlet 12, walk in the tubulation pipe, and heat exchanger upper inlet 15 enter away between the tubulation pipe part (1/3) high temperature shift gas and stream and descend, carry out heat exchange, be heated to rapidly away from going out by lower part outlet 13 after the dew-point temperature, reenter main heat exchanger 11 bottoms, go out from top outlet 14 to the upper reaches, with advance from main heat exchanger 11 tops 17, high temperature shift gas between the pipe that bottom 18 exports out (2/3 conversion gas) carries out counterflow heat exchange, is heated to processing requirement temperature (going into the temperature of shift converter).19 are the temperature adjustment by-pass.Low temperature shift gas after large and small thermal converter heat exchange goes down operation.
Before main heat exchanger, add the pre-etching heat exchanger, can avoid main heat exchanger to suffer the wet gas dew point corrosion, reduce and change main heat exchanger number of times, cost saving.
This saturated coal gas and conversion gas heat exchange anti-corrosion method and equipment, other similarly prevent dew point corrosion also to be applicable to oil, chemical industry etc., or the occasion of local generation heavy corrosion.
Claims (4)
1, saturated coal gas and conversion gas heat exchange anti-corrosion method, it is characterized in that with 1/3 conversion gas and the saturated coal gas of low temperature and flow heat exchange, improve saturated gas temperature rapidly, make saturated coal gas be heated into unsaturation wet gas away from dew point, avoid dew point corrosion, wet gas counterflow heat exchange with after 2/3 conversion gas and the temperature raising is heated to the processing requirement temperature with wet gas.
2, the equipment that is used for the described method of claim 1, and adverse current tubular heat exchanger, by cylindrical shell (1), tubulation (2), tube sheet (3) and traverse baffle (4) are formed, tubulation (2) two is fixed on and is installed in the cylindrical shell (1) on the tube sheet (3), tubulation (3) pipe saturated coal gas interior and cylindrical shell (1) two is imported and exported (5), (6) communicate, traverse baffle (4) is partitioned into the baffling passage with pipe, there is conversion gas master import (7) at baffling passage two on cylindrical shell (1), outlet (9), it is characterized in that going up the secondary import (8) of conversion gas in addition at cylindrical shell (1), saturated coal gas becomes and flow structure from import (5) to outlet (6) pipe interior passageway with the tube lane of conversion gas from secondary import (8) to outlet (9), and stream heat exchange segment, become counterflow configuration, the counterflow heat exchange section with the tube lane of conversion gas from main import (9) to outlet (9).
3, equipment as claimed in claim 2 is characterized in that and flow heat exchange segment that 2 traverse baffles (4) are arranged.
4, equipment as claimed in claim 2 is characterized in that and the heat exchange area that flows heat exchange segment accounts for 1/5 of the total heat exchange area of equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95112522A CN1067656C (en) | 1995-11-01 | 1995-11-01 | Anti-corrosive method and apparatus by heat exchange of saturated gas with changing gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95112522A CN1067656C (en) | 1995-11-01 | 1995-11-01 | Anti-corrosive method and apparatus by heat exchange of saturated gas with changing gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1126176A CN1126176A (en) | 1996-07-10 |
| CN1067656C true CN1067656C (en) | 2001-06-27 |
Family
ID=5079589
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95112522A Expired - Lifetime CN1067656C (en) | 1995-11-01 | 1995-11-01 | Anti-corrosive method and apparatus by heat exchange of saturated gas with changing gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1067656C (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102500282B (en) * | 2011-11-04 | 2014-04-09 | 神华集团有限责任公司 | Coal purifying equipment changing pipeline and anticracking method thereof |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4308066C1 (en) * | 1993-03-13 | 1994-06-01 | Uhde Gmbh | Cleaning ammonia evaporator - by thermal decomposition of ammonium-contg. deposits |
-
1995
- 1995-11-01 CN CN95112522A patent/CN1067656C/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4308066C1 (en) * | 1993-03-13 | 1994-06-01 | Uhde Gmbh | Cleaning ammonia evaporator - by thermal decomposition of ammonium-contg. deposits |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1126176A (en) | 1996-07-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN207439189U (en) | A kind of exhaust steam afterheat recycling device for aerated brick field | |
| CN102141253A (en) | Phase transition combined air preheater | |
| CN2847159Y (en) | Utilizing device for boiler smoke waste heat | |
| CN2368001Y (en) | Integrated heat-pipe type compound phase transition heat exchanger | |
| CN101261008B (en) | Liquid phase intermediate medium heat exchanging type heat exchanger | |
| CN206950989U (en) | A kind of VOCs exhaust fume catalytics oxidation furnaces | |
| CN1067656C (en) | Anti-corrosive method and apparatus by heat exchange of saturated gas with changing gas | |
| CN201373673Y (en) | Condenser with longitudinal separation plate and inclined supporting plate | |
| CN201206829Y (en) | Liquid phase intermediate medium heat exchanging type heat exchanger | |
| CN217519888U (en) | Flue gas waste heat recovery gas heat exchange device based on heat medium is water | |
| CN203719469U (en) | Pressure-bearing smoke waste heat exchanger | |
| CN205227896U (en) | Condensate water is recovery system again | |
| CN205115337U (en) | Low power consuming is by device of methyl alcohol preparation aerosol dimethyl ether | |
| CN205245115U (en) | Novel gasifier with burn burning furnace exhaust -heat boiler | |
| CN2140045Y (en) | Clip cover type collision cross section-changing flow cylinder baffle heat exchanger | |
| CN206055582U (en) | A kind of synthesis ammonia plug-in type waste heat boiler | |
| CN1378059A (en) | Water heating method and device without scaling and resisting high pressure | |
| CN202002140U (en) | Forced circulation air preheating system | |
| CN102012039A (en) | Forced circulation air preheat system | |
| CN105371512B (en) | Condensate recycling system | |
| CN201392111Y (en) | Crude oil/steam heat exchanger | |
| CN218458675U (en) | Built-in tower top condensing device | |
| CN2585119Y (en) | Device for water heating without scale and with high pressure resistance | |
| CN210862319U (en) | High-efficient gas heater | |
| CN211585886U (en) | White smoke device that disappears of mixing wind is cooled off to wet flue gas desulfurization tower inner loop thick liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: HUASHUO SCIENCE AND TECHNOLOGY CO., LTD. Free format text: FORMER NAME: HUBEI CHEMICAL RESEARCH INSTITUTE |
|
| CP01 | Change in the name or title of a patent holder |
Address after: Hubei Province, Wuhan City, Wuchang mountain Patentee after: Huashuo Technology Co., Ltd. Address before: Hubei Province, Wuhan City, Wuchang mountain Patentee before: Hubei Research Institute of Chemistry |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Anti-corrosive method and apparatus by heat exchange of saturated gas with changing gas Effective date of registration: 20100907 Granted publication date: 20010627 Pledgee: Bank of Hankou, Limited by Share Ltd, Optics Valley branch Pledgor: Huashuo Technology Co., Ltd. Registration number: 2010990000869 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20151106 Granted publication date: 20010627 Pledgee: Bank of Hankou Limited by Share Ltd Optics Valley branch Pledgor: Huashuo Technology Co., Ltd. Registration number: 2010990000869 |
|
| PLDC | Enforcement, change and cancellation of contracts on pledge of patent right or utility model | ||
| PM01 | Change of the registration of the contract for pledge of patent right |
Change date: 20151106 Registration number: 2010990000869 Pledgee after: Bank of Hankou Limited by Share Ltd Optics Valley branch Pledgee before: Bank of Hankou, Limited by Share Ltd, Optics Valley branch |
|
| CX01 | Expiry of patent term |
Granted publication date: 20010627 |
|
| EXPY | Termination of patent right or utility model |