CN104828775B - A device used for CO gas conversion and cooling - Google Patents
A device used for CO gas conversion and cooling Download PDFInfo
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- CN104828775B CN104828775B CN201510128418.5A CN201510128418A CN104828775B CN 104828775 B CN104828775 B CN 104828775B CN 201510128418 A CN201510128418 A CN 201510128418A CN 104828775 B CN104828775 B CN 104828775B
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- cooler
- thermal converter
- outlet end
- lime set
- export
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- 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
- Y02P20/10—Process efficiency
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- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention relates to a gas conversion and cooling device, and particularly relates to a device used for CO gas conversion and cooling. The objective of the invention is to overcome the problem that the efficiency of converting CO gas into H2 of CO gas conversion and cooling devices at present is low and cannot meet requirements of methanol synthesis devices and the problem that the heat recovery rate is low. Raw gas is fed from a raw gas compressor to a degreaser, a preheating converter, a main-heat converter, a first converting furnace, a medium-pressure waste heat recoverer, the main-heat converter, a separator, a second converting furnace, a sub-medium pressure waste heat recoverer, the preheating converter, a boiler feed water preheater, a desalted water preheater, a cooler, an amino washing separating tower, a stripping tower, a condensate heat exchanger, a condensate cooler, a final cooler and a gasification circulating water pipe in order to perform a conversion reaction. The device is suitable for conversion reactions.
Description
Technical field
The present invention relates to the device of a kind of conversion of gas and cooling.
Background technology
Being becoming tight petroleum resources day in recent years affects, and China's Coal Chemical Industry enters Rapid development stage.In view of air-flow bed coal-gasification
Technology has many advantages, such as that, synthesis gas active component low to coal quality requirements is high and operating cost is low, becomes modern coal gasification skill
The major fields of art development.
CO conversion process is widely used on synthetic ammonia installation and device for producing hydrogen, belongs to a major part purifying technique,
After its process station is arranged on gasification or conversion procedure.Different conversion process is mainly reflected in transformationreation hop count, reaction
Temperature, the change of heat recovery three aspect, this depends primarily on the performance of transformation catalyst, and the hydrogen manufacturing that commercial production adopts is former
The factors such as material, process for making hydrogen, subsequent purification technique.
The waste heat recovery of traditional CO conversion process typically takes quenching to be humidified, and in the form of latent heat, reaction heat is used in other
On the conversion gas reboiler of operation, it is provided with other heat reclamation devices of setting；Energy-saving flow process then eliminates quenching, sets up de-
Carbon injection steam generator, simultaneously as far as possible many reclaim low changing air used heat using multiple conversion gas reboilers, and use low pressure cooker
Stove feed-water heater fully reclaims the sensible heat of low change and latent heat, is not provided with other heat reclamation devices.
Content of the invention
The invention aims to solving existing CO gas conversion and the device of cooling is H by CO gas conversion2Efficiency
Low it is impossible to meet the demand of methanol synthesizer and the problem that heat recovery rate is low, and provide a kind of for CO gas conversion and
The device of cooling.
A kind of device for CO gas conversion and cooling includes rough coal air compressor, grease trap, pre- thermal converter, main heat
Changer, secondary middle discard heat regenerator, middle discard heat regenerator, the first change furnace, separator, the second change furnace, boiler
Feed water preheater, desalination water preheater, cooler, wash ammonia separation tower, stripper, lime set heat exchanger, lime set cooler and
Gasification cycle water pipe；
Described pre- thermal converter includes pre- thermal converter first entrance end, pre- thermal converter second entrance end, pre- thermal converter
First outlet end and pre- thermal converter second outlet end；
Described main thermal converter includes main thermal converter first entrance end, main thermal converter second entrance end, main thermal converter
First outlet end and main thermal converter second outlet end；
Described lime set cooler includes lime set cooler arrival end, lime set cooler first outlet end, lime set cooler second
The port of export and lime set cooler the 3rd port of export；
Described ammonia separation tower of washing includes washing ammonia separation tower arrival end, washes ammonia separation tower first outlet end and wash ammonia separation tower second
Arrival end；
Described cooler includes cooler arrival end, cooler first outlet end and cooler second outlet end；
The described port of export of rough coal air compressor is connected with the arrival end of grease trap；The port of export of grease trap and pre- thermal conversion
Device first entrance end is connected；Pre- thermal converter first outlet end is connected with main thermal converter first entrance end；Main thermal conversion
Device first outlet end is connected with the arrival end of the first change furnace；First change furnace is by middle discard heat regenerator and main thermal conversion
Device second entrance end is connected；Main thermal converter second outlet end is connected with the arrival end of separator；The port of export of separator
It is connected with the arrival end of the second change furnace, the second change furnace passes through time middle discard heat regenerator and pre- thermal converter second entrance
End is connected；Pre- thermal converter second outlet end is connected with the arrival end of feedwater preheater；Feedwater preheater
The port of export is connected with the arrival end of desalination water preheater；The port of export of desalination water preheater passes through cooler and washes ammonia separation tower
Arrival end is connected；Wash ammonia separation tower first outlet end to be connected with lime set heat exchanger by stripper；The going out of lime set heat exchanger
Mouth end is connected with lime set cooler arrival end；Lime set cooler first outlet end is connected with cooler second outlet end；Solidifying
Liquid cooler second outlet end is connected with washing ammonia separation tower second entrance end；Lime set cooler the 3rd port of export and gasification cycle
Water pipe is connected.
Advantages of the present invention：
First, steam consumption of the present invention is low；
2nd, change furnace inlet temperature of the present invention is low, thickness that is reducing equipment；
3rd, the present invention is provided with catalyst layer in the first change furnace and the second change furnace, loads resistant to sulfur catalyst catalyst, resistant to sulfur
Catalyst contains 1.8%Co0 and 8.0%Mo0, and catalyst filling amount greatly reduces, and reduces bed resistance, improves conversion
The capacity of equipment of stove；
4th, present device smooth operation, overcomes the malaria of middle temperature transformation, decreases equipment size, reduce equipment
Expense；
5th, the present invention improves the conversion capability of organic sulfur；
6th, the present invention solves existing CO gas conversion and the device of cooling is H by CO gas conversion2Low the asking of efficiency
Topic, the gas after conversion can meet the demand of methanol synthesizer；Heat recovery rate of the present invention is high.
The present invention is applied to transformationreation.
Brief description
Fig. 1 is the installation drawing for CO gas conversion and cooling described in specific embodiment one.
Specific embodiment
Specific embodiment one：Present embodiment is that a kind of device for CO gas conversion and cooling includes raw gas compression
Machine 1, grease trap 2, pre- thermal converter 3, main thermal converter 4, secondary middle discard heat regenerator 5, middle discard heat regenerator 6,
First change furnace 7, separator 8, the second change furnace 9, feedwater preheater 10, desalination water preheater 11, cooler
12nd, ammonia separation tower 13, stripper 14, lime set heat exchanger 15, lime set cooler 16 and gasification circulating water pipe 17 are washed；
Described pre- thermal converter 3 include pre- thermal converter first entrance end 3-1, pre- thermal converter second entrance end 3-2,
Pre- thermal converter first outlet end 3-3 and pre- thermal converter second outlet end 3-4；
Described main thermal converter 4 include main thermal converter first entrance end 4-1, main thermal converter second entrance end 4-2,
Main thermal converter first outlet end 4-3 and main thermal converter second outlet end 4-4；
Described lime set cooler 16 includes lime set cooler arrival end 16-1, lime set cooler first outlet end 16-2, coagulates
Liquid cooler second outlet end 16-3 and lime set cooler the 3rd port of export 16-4；
Described ammonia separation tower 13 of washing includes washing ammonia separation tower arrival end 13-1, washes ammonia separation tower first outlet end 13-2 and wash
Ammonia separation tower second entrance end 13-3；
Described cooler 12 includes cooler arrival end 12-1, cooler first outlet end 12-2 and cooler second outlet
End 12-3；
The described port of export of rough coal air compressor 1 is connected with the arrival end of grease trap 2；The port of export of grease trap 2 with pre-
Thermal converter first entrance end 3-1 is connected；Pre- thermal converter first outlet end 3-3 and main thermal converter first entrance end 4-1
It is connected；Main thermal converter first outlet end 4-3 is connected with the arrival end of the first change furnace 7；First change furnace 7 passes through
Middle discard heat regenerator 6 is connected with main thermal converter second entrance end 4-2；Main thermal converter second outlet end 4-4 with point
Arrival end from device 8 is connected；The port of export of separator 8 is connected with the arrival end of the second change furnace 9, the second change furnace
9 are connected with pre- thermal converter second entrance end 3-2 by time middle discard heat regenerator 5；Pre- thermal converter second outlet end
3-4 is connected with the arrival end of feedwater preheater 10；The port of export of feedwater preheater 10 and desalination water preheater
11 arrival end is connected；The port of export of desalination water preheater 11 passes through cooler 12 and washes ammonia separation tower arrival end 13-1
It is connected；Wash ammonia separation tower first outlet end 13-2 to be connected with lime set heat exchanger 15 by stripper 14；Lime set heat exchange
The port of export of device 15 is connected with lime set cooler arrival end 16-1；Lime set cooler first outlet end 16-2 and cooler
Second outlet end 12-3 is connected；Lime set cooler second outlet end 16-3 with wash ammonia separation tower second entrance end 13-3 phase
Connection；Lime set cooler the 3rd port of export 16-4 is connected with gasification cycle water pipe 17.
Fig. 1 is the installation drawing for CO gas conversion and cooling described in specific embodiment one；In Fig. 1,1 is raw gas
Compressor, 2 is grease trap, and 3 is pre- thermal converter, thermal converter based on 4, and 5 is time middle discard heat regenerator, during 6 are
Discard heat regenerator, 7 is the first change furnace, and 8 is separator, and 9 is the second change furnace, and 10 is feedwater preheater,
11 is desalination water preheater, and 12 is cooler, and 13 is to wash ammonia separation tower, and 14 is stripper, and 15 is lime set heat exchanger,
16 is lime set cooler, and 17 is gasification cycle water pipe, and 3-1 is pre- thermal converter first entrance end, and 3-2 is pre- thermal converter
Second entrance end, 3-3 is pre- thermal converter first outlet end, and 3-4 is pre- thermal converter second outlet end, and based on 4-1, heat becomes
Parallel operation first entrance end, thermal converter second entrance end based on 4-2, thermal converter first outlet end based on 4-3, based on 4-4
Thermal converter second outlet end, 16-1 is lime set cooler arrival end, and 16-2 is lime set cooler first outlet end, 16-3
For lime set cooler second outlet end, 13-1 is to wash ammonia separation tower, and 13-2 is to wash ammonia separation tower first outlet end, and 13-3 is
Wash ammonia separation tower second entrance end, 12-1 is cooler arrival end, 12-2 is cooler first outlet end, 12-3 is cooling
Device second outlet end.
The advantage of present embodiment：
First, present embodiment steam consumption is low；
2nd, present embodiment change furnace inlet temperature is low, reduce the thickness of equipment；
3rd, present embodiment is provided with catalyst layer in the first change furnace 7 and the second change furnace 9, loads the catalysis of resistant to sulfur catalyst
Agent, resistant to sulfur catalyst contains 1.8%Co0 and 8.0%Mo0, and catalyst filling amount greatly reduces, and reduces bed resistance, carries
The high capacity of equipment of change furnace；
4th, present embodiment equipment operation steadily, overcomes the malaria of middle temperature transformation, decreases equipment size, reduce
Cost of equipment；
5th, present embodiment improves the conversion capability of organic sulfur；
6th, present embodiment solves existing CO gas conversion and the device of cooling is H by CO gas conversion2Efficiency low
Problem, the gas after conversion can meet the demand of methanol synthesizer；Present embodiment heat recovery rate is high.
Present embodiment is applied to transformationreation.
Specific embodiment two：Present embodiment with specific embodiment one difference is：Described grease trap 2 is provided with first mate
Line, can purge to it in the case of not parking.Other steps are identical with specific embodiment one.
Specific embodiment three：Present embodiment with one of specific embodiment one or two difference is：Described pre- thermal conversion
On the conversion gas by-pass of device 3, setting adjusts the valve of coal gas.Other steps are identical with specific embodiment one or two.
Specific embodiment four：Present embodiment with one of specific embodiment one to three difference is：Described main thermal conversion
On the conversion gas by-pass of device 4, setting adjusts the valve of coal gas.Other steps are identical with specific embodiment one to three.
Specific embodiment five：Present embodiment with one of specific embodiment one to four difference is：Described rough coal air pressure
The pressure of contracting machine 1 is 4.0MPaG.Other steps are identical with specific embodiment one to four.
Specific embodiment six：Present embodiment with one of specific embodiment one to five difference is：Described cooler
12 is shell-and-tube fixed tube-sheet exchanger.Other steps are identical with specific embodiment one to five.
Specific embodiment seven：Present embodiment with one of specific embodiment one to six difference is：The first described conversion
It is provided with catalyst layer in stove 7；Catalyst in described catalyst layer is resistant to sulfur catalyst；Described resistant to sulfur catalyst contains 1.8%
Co0 and 8.0%Mo0.Other steps are identical with specific embodiment one to six.
Specific embodiment eight：Present embodiment with one of specific embodiment one to seven difference is：The second described conversion
It is provided with catalyst layer in stove 9；Catalyst in described catalyst layer is resistant to sulfur catalyst；Described resistant to sulfur catalyst contains 1.8%
Co0 and 8.0%Mo0.Other steps are identical with specific embodiment one to seven.
Claims (1)
1. a kind of for CO gas conversion and cooling device it is characterised in that described device include rough coal air compressor (1),
Grease trap (2), pre- thermal converter (3), main thermal converter (4), secondary middle discard heat regenerator (5), middle discard recuperation of heat
Device (6), the first change furnace (7), separator (8), the second change furnace (9), feedwater preheater (10), desalted water
Preheater (11), cooler (12), to wash ammonia separation tower (13), stripper (14), lime set heat exchanger (15), lime set cold
But device (16) and gasification circulating water pipe (17)；
Described pre- thermal converter (3) include pre- thermal converter first entrance end (3-1), pre- thermal converter second entrance end (3-2),
Pre- thermal converter first outlet end (3-3) and pre- thermal converter second outlet end (3-4)；
Described main thermal converter (4) include main thermal converter first entrance end (4-1), main thermal converter second entrance end (4-2),
Main thermal converter first outlet end (4-3) and main thermal converter second outlet end (4-4)；
Described lime set cooler (16) include lime set cooler arrival end (16-1), lime set cooler first outlet end (16-2),
Lime set cooler second outlet end (16-3) and lime set cooler the 3rd port of export (16-4)；
Described ammonia separation tower (13) of washing includes washing ammonia separation tower arrival end (13-1), washing ammonia separation tower first outlet end (13-2)
With wash ammonia separation tower second entrance end (13-3)；
Described cooler (12) includes cooler arrival end (12-1), cooler first outlet end (12-2) and cooler
Second outlet end (12-3)；
The described port of export of rough coal air compressor (1) is connected with the arrival end of grease trap (2)；The going out of grease trap (2)
Mouth end is connected with pre- thermal converter first entrance end (3-1)；Pre- thermal converter first outlet end (3-3) and main thermal converter
(4-1) is connected at first entrance end；The arrival end phase of main thermal converter first outlet end (4-3) and the first change furnace (7)
Connection；First change furnace (7) is connected with main thermal converter second entrance end (4-2) by middle discard heat regenerator (6)；
Main thermal converter second outlet end (4-4) is connected with the arrival end of separator (8)；The port of export of separator (8) and
The arrival end of two change furnaces (9) is connected, and the second change furnace (9) passes through time middle discard heat regenerator (5) and pre- thermal conversion
Device second entrance end (3-2) is connected；Pre- thermal converter second outlet end (3-4) is entered with feedwater preheater (10)
Mouth end is connected；The port of export of feedwater preheater (10) is connected with the arrival end of desalination water preheater (11)；De-
The port of export of brine preheater (11) is connected with washing ammonia separation tower arrival end (13-1) by cooler (12)；Wash ammonia
Knockout tower first outlet end (13-2) is connected with lime set heat exchanger (15) by stripper (14)；Lime set heat exchanger (15)
The port of export be connected with lime set cooler arrival end (16-1)；Lime set cooler first outlet end (16-2) and cooler the
Two ports of export (12-3) are connected；Lime set cooler second outlet end (16-3) with wash ammonia separation tower second entrance end (13-3)
It is connected；Lime set cooler the 3rd port of export (16-4) is connected with gasification cycle water pipe (17)；
Described grease trap (2) is provided with big by-pass, in the case of not parking, it can be purged；
On the described conversion gas by-pass of pre- thermal converter (3), setting adjusts the valve of coal gas；
On the described conversion gas by-pass of main thermal converter (4), setting adjusts the valve of coal gas；
The pressure of described rough coal air compressor (1) is 4.0MPaG；
Described cooler (12) is shell-and-tube fixed tube-sheet exchanger；
It is provided with catalyst layer in described the first change furnace (7)；Catalyst in described catalyst layer is resistant to sulfur catalyst；Institute
The resistant to sulfur catalyst stated contains 1.8%CoO and 8.0%MoO；
It is provided with catalyst layer in described the second change furnace (9)；Catalyst in described catalyst layer is resistant to sulfur catalyst；Institute
The resistant to sulfur catalyst stated contains 1.8%CoO and 8.0%MoO.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510128418.5A CN104828775B (en) | 2015-03-23 | 2015-03-23 | A device used for CO gas conversion and cooling |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510128418.5A CN104828775B (en) | 2015-03-23 | 2015-03-23 | A device used for CO gas conversion and cooling |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104828775A CN104828775A (en) | 2015-08-12 |
| CN104828775B true CN104828775B (en) | 2017-02-08 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510128418.5A Active CN104828775B (en) | 2015-03-23 | 2015-03-23 | A device used for CO gas conversion and cooling |
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Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108862195B (en) * | 2018-06-19 | 2022-07-19 | 中国石油化工股份有限公司 | Coal gas-making sulfur-tolerant conversion system capable of improving stopping and starting work cooling efficiency |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2709768A1 (en) * | 1977-03-07 | 1978-09-21 | Metallgesellschaft Ag | METHOD FOR CATALYTICALLY CONVERTING RAW GAS FROM THE GASIFICATION OF SOLID FUELS |
| CN101157442B (en) * | 2007-04-27 | 2010-07-21 | 中国石化集团宁波工程有限公司 | Waste heat reclaiming process for CO transformation |
| CN101434379B (en) * | 2008-12-15 | 2011-07-13 | 四川天一科技股份有限公司 | Coke-oven gas transform processing method |
| FR2943656A1 (en) * | 2009-03-25 | 2010-10-01 | Air Liquide | HYDROGEN PRODUCTION METHOD AND PLANT USING A THERMOCINETIC COMPRESSOR |
| CN103435006B (en) * | 2013-08-20 | 2015-04-08 | 湖南安淳高新技术有限公司 | High-CO high-conversion-rate isothermal shift reactor |
| CN204454564U (en) * | 2015-03-23 | 2015-07-08 | 七台河宝泰隆煤化工股份有限公司 | A kind of device for CO gas conversion and cooling |
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Address after: 154603 Heilongjiang city of Qitaihe Province New District baotailong Road No. 16 Applicant after: Baotailong new materials Limited by Share Ltd Address before: 154603 Heilongjiang city of Qitaihe Province New District baotailong Road No. 16 Applicant before: Coal Chemical Industry Company Limited by Shares of the precious ACE Semi of Qitaihe |
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