CN104828775A - 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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- CN104828775A CN104828775A CN201510128418.5A CN201510128418A CN104828775A CN 104828775 A CN104828775 A CN 104828775A CN 201510128418 A CN201510128418 A CN 201510128418A CN 104828775 A CN104828775 A CN 104828775A
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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 a kind of conversion of gas and the device of cooling.
Background technology
Be becoming tight by petroleum resources day in recent years and affect, China's Coal Chemical Industry enters Rapid development stage.In view of air-flow bed coal-gasification technology has the plurality of advantages such as low to coal quality requirements, synthetic gas active principle is high and working cost is low, become the major fields of modern Coal Gasification Technology development.
CO conversion process is widely used on synthetic ammonia installation and device for producing hydrogen, belongs to a major portion of purification process, after its process station is arranged on gasification or conversion procedure.Different conversion process is mainly reflected in transformationreation hop count, the change of temperature of reaction, heat recuperation three aspect, and this depends primarily on the performance of transformation catalyst, the factor such as hydrogen feedstock, process for making hydrogen, subsequent purification technique that industrial production adopts.
The waste heat recovery of traditional CO conversion process generally takes quenching to be humidified, and with the form of latent heat, reaction heat is used on the conversion gas reboiler of other operation, is provided with and arranges other heat reclamation devices; Energy-saving flow process then eliminates quenching, set up decarburization uperize producer, the multiple conversion gas reboiler of simultaneously as far as possible many employings reclaims low changing air used heat, and with low pressure boiler feedwater heating apparatus, the sensible heat of low change and latent heat is fully reclaimed, and does not arrange other heat reclamation device.
Summary of the invention
CO gas conversion is H by the device that the object of the invention is to solve existing CO gas conversion and cooling
2efficiency low, the demand of methanol synthesizer and the low problem of heat recovery rate can not be met, and a kind of device for CO gas conversion and cooling is provided.
A kind of device for CO gas conversion and cooling comprises raw gas compressor, oil eliminator, pre-thermal converter, main thermal converter, secondary middle pressure waste-heat recoverer, middle pressure waste-heat recoverer, the first shift converter, separator, the second shift converter, feedwater preheater, de-salted water preheater, water cooler, washes ammonia separation tower, stripping tower, lime set interchanger, lime set water cooler and gasification circulating pipe;
Described pre-thermal converter comprises pre-thermal converter first inlet end, pre-thermal converter second inlet end, pre-thermal converter first exit end and pre-thermal converter second exit end;
Described main thermal converter comprises main thermal converter first inlet end, main thermal converter second inlet end, main thermal converter first exit end and main thermal converter second exit end;
Described lime set water cooler comprises lime set water cooler inlet end, lime set water cooler first exit end, lime set water cooler second exit end and lime set water cooler the 3rd exit end;
Described ammonia separation tower of washing comprises and washes ammonia separation tower inlet end, washes ammonia separation tower first exit end and wash ammonia separation tower second inlet end;
Described water cooler comprises water cooler inlet end, water cooler first exit end and water cooler second exit end;
The described exit end of raw gas compressor is connected with the inlet end of oil eliminator; The exit end of oil eliminator is connected with pre-thermal converter first inlet end; Pre-thermal converter first exit end is connected with main thermal converter first inlet end; Main thermal converter first exit end is connected with the inlet end of the first shift converter; First shift converter is connected with main thermal converter second inlet end by middle pressure waste-heat recoverer; Main thermal converter second exit end is connected with the inlet end of separator; The exit end of separator is connected with the inlet end of the second shift converter, and the second shift converter is connected with pre-thermal converter second inlet end by time middle pressure waste-heat recoverer; Pre-thermal converter second exit end is connected with the inlet end of feedwater preheater; The exit end of feedwater preheater is connected with the inlet end of de-salted water preheater; The exit end of de-salted water preheater by water cooler with wash ammonia separation tower inlet end and be connected; Wash ammonia separation tower first exit end to be connected with lime set interchanger by stripping tower; The exit end of lime set interchanger is connected with lime set water cooler inlet end; Lime set water cooler first exit end is connected with water cooler second exit end; Lime set water cooler second exit end with wash ammonia separation tower second inlet end and be connected; Lime set water cooler the 3rd exit end is connected with gasification cycle water pipe.
Advantage of the present invention:
One, steam consumption of the present invention is low;
Two, low, the thickness that reduces equipment of shift converter temperature in of the present invention;
Three, the present invention is provided with catalyst layer in the first shift converter and the second shift converter, and load resistant to sulfur catalyst catalyzer, resistant to sulfur catalyst contains 1.8%Co0 and 8.0%Mo0, and catalyst filling amount greatly reduces, and reduces bed resistance, improves the capacity of equipment of shift converter;
Four, present device smooth operation, overcomes the malaria of middle temperature transformation, decreases equipment size, reduce cost of equipment;
Five, invention increases the conversion capability of organosulfur;
Six, the present invention solves the device of existing CO gas conversion and cooling is H by CO gas conversion
2inefficient problem, the gas after conversion can meet the demand of methanol synthesizer; Heat recovery rate of the present invention is high.
The present invention is applicable to transformationreation.
Accompanying drawing explanation
Fig. 1 is the setting drawing for CO gas conversion and cooling described in embodiment one.
Embodiment
Embodiment one: present embodiment is that a kind of device for CO gas conversion and cooling comprises raw gas compressor 1, oil eliminator 2, pre-thermal converter 3, main thermal converter 4, secondary middle pressure waste-heat recoverer 5, middle pressure waste-heat recoverer 6, first shift converter 7, separator 8, second shift converter 9, feedwater preheater 10, de-salted water preheater 11, water cooler 12, washes ammonia separation tower 13, stripping tower 14, lime set interchanger 15, lime set water cooler 16 and gasification circulating pipe 17;
Described pre-thermal converter 3 comprises pre-thermal converter first inlet end 3-1, pre-thermal converter second inlet end 3-2, pre-thermal converter first exit end 3-3 and pre-thermal converter second exit end 3-4;
Described main thermal converter 4 comprises main thermal converter first inlet end 4-1, main thermal converter second inlet end 4-2, main thermal converter first exit end 4-3 and main thermal converter second exit end 4-4;
Described lime set water cooler 16 comprises lime set water cooler inlet end 16-1, lime set water cooler first exit end 16-2, lime set water cooler second exit end 16-3 and lime set water cooler the 3rd exit end 16-4;
Described ammonia separation tower 13 of washing comprises and washes ammonia separation tower inlet end 13-1, washes ammonia separation tower first exit end 13-2 and wash ammonia separation tower second inlet end 13-3;
Described water cooler 12 comprises water cooler inlet end 12-1, water cooler first exit end 12-2 and water cooler second exit end 12-3;
The exit end of described raw gas compressor 1 is connected with the inlet end of oil eliminator 2; The exit end of oil eliminator 2 is connected with pre-thermal converter first inlet end 3-1; Pre-thermal converter first exit end 3-3 is connected with main thermal converter first inlet end 4-1; Main thermal converter first exit end 4-3 is connected with the inlet end of the first shift converter 7; First shift converter 7 is connected with main thermal converter second inlet end 4-2 by middle pressure waste-heat recoverer 6; Main thermal converter second exit end 4-4 is connected with the inlet end of separator 8; The exit end of separator 8 is connected with the inlet end of the second shift converter 9, and the second shift converter 9 is connected with pre-thermal converter second inlet end 3-2 by time middle pressure waste-heat recoverer 5; Pre-thermal converter second exit end 3-4 is connected with the inlet end of feedwater preheater 10; The exit end of feedwater preheater 10 is connected with the inlet end of de-salted water preheater 11; The exit end of de-salted water preheater 11 by water cooler 12 with wash ammonia separation tower inlet end 13-1 and be connected; Wash ammonia separation tower first exit end 13-2 to be connected with lime set interchanger 15 by stripping tower 14; The exit end of lime set interchanger 15 is connected with lime set water cooler inlet end 16-1; Lime set water cooler first exit end 16-2 is connected with water cooler second exit end 12-3; Lime set water cooler second exit end 16-3 with wash ammonia separation tower second inlet end 13-3 and be connected; Lime set water cooler the 3rd exit end 16-4 is connected with gasification cycle water pipe 17.
Fig. 1 is the setting drawing for CO gas conversion and cooling described in embodiment one, in Fig. 1,1 is raw gas compressor, 2 is oil eliminator, 3 is pre-thermal converter, 4 is main thermal converter, 5 is time middle pressure waste-heat recoverer, 6 is middle pressure waste-heat recoverer, 7 is the first shift converter, 8 is separator, 9 is the second shift converter, 10 is feedwater preheater, 11 is de-salted water preheater, 12 is water cooler, 13 for washing ammonia separation tower, 14 is stripping tower, 15 is lime set interchanger, 16 is lime set water cooler, 17 is gasification cycle water pipe, 3-1 is pre-thermal converter first inlet end, 3-2 is pre-thermal converter second inlet end, 3-3 is pre-thermal converter first exit end, 3-4 is pre-thermal converter second exit end, 4-1 is main thermal converter first inlet end, 4-2 is main thermal converter second inlet end, 4-3 is main thermal converter first exit end, 4-4 is main thermal converter second exit end, 16-1 is lime set water cooler inlet end, 16-2 is lime set water cooler first exit end, 16-3 is lime set water cooler second exit end, 13-1 is for washing ammonia separation tower, 13-2 is for washing ammonia separation tower first exit end, 13-3 is for washing ammonia separation tower second inlet end, 12-1 is water cooler inlet end, 12-2 is water cooler first exit end, 12-3 is water cooler second exit end.
The advantage of present embodiment:
One, present embodiment steam consumption is low;
Two, low, the thickness that reduces equipment of present embodiment shift converter temperature in;
Three, present embodiment is provided with catalyst layer in the first shift converter 7 and the second shift converter 9, load resistant to sulfur catalyst catalyzer, resistant to sulfur catalyst contains 1.8%Co0 and 8.0%Mo0, and catalyst filling amount greatly reduces, reduce bed resistance, improve the capacity of equipment of shift converter;
Four, present embodiment operation of equipment is steady, overcomes the malaria of middle temperature transformation, decreases equipment size, reduce cost of equipment;
Five, present embodiment improves the conversion capability of organosulfur;
Six, present embodiment solves the device of existing CO gas conversion and cooling is H by CO gas conversion
2inefficient problem, the gas after conversion can meet the demand of methanol synthesizer; Present embodiment heat recovery rate is high.
Present embodiment is applicable to transformationreation.
Embodiment two: present embodiment and embodiment one difference are: described oil eliminator 2 is provided with large by-pass, can purge when not stopping to it.Other steps are identical with embodiment one.
Embodiment three: one of present embodiment and embodiment one or two difference is: the conversion gas by-pass of described pre-thermal converter 3 arranges the valve regulating coal gas.Other steps are identical with embodiment one or two.
Embodiment four: one of present embodiment and embodiment one to three difference is: the conversion gas by-pass of described main thermal converter 4 is arranged the valve regulating coal gas.Other steps are identical with embodiment one to three.
Embodiment five: one of present embodiment and embodiment one to four difference is: the pressure of described raw gas compressor 1 is 4.0MPaG.Other steps are identical with embodiment one to four.
Embodiment six: one of present embodiment and embodiment one to five difference is: described water cooler 12 is shell-and-tube fixed tube-sheet heat exchanger.Other steps are identical with embodiment one to five.
Embodiment seven: one of present embodiment and embodiment one to six difference is: be provided with catalyst layer in the first described shift converter 7; Catalyzer 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 embodiment one to six.
Embodiment eight: one of present embodiment and embodiment one to seven difference is: be provided with catalyst layer in the second described shift converter 9; Catalyzer 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 embodiment one to seven.
Claims (8)
1. the device for CO gas conversion and cooling, it is characterized in that a kind of device for CO gas conversion and cooling comprises raw gas compressor (1), oil eliminator (2), pre-thermal converter (3), main thermal converter (4), secondary middle pressure waste-heat recoverer (5), middle pressure waste-heat recoverer (6), first shift converter (7), separator (8), second shift converter (9), feedwater preheater (10), de-salted water preheater (11), water cooler (12), wash ammonia separation tower (13), stripping tower (14), lime set interchanger (15), lime set water cooler (16) and gasification circulating pipe (17),
Described pre-thermal converter (3) comprises pre-thermal converter first inlet end (3-1), pre-thermal converter second inlet end (3-2), pre-thermal converter first exit end (3-3) and pre-thermal converter second exit end (3-4);
Described main thermal converter (4) comprises main thermal converter first inlet end (4-1), main thermal converter second inlet end (4-2), main thermal converter first exit end (4-3) and main thermal converter second exit end (4-4);
Described lime set water cooler (16) comprises lime set water cooler inlet end (16-1), lime set water cooler first exit end (16-2), lime set water cooler second exit end (16-3) and lime set water cooler the 3rd exit end (16-4);
Described ammonia separation tower (13) of washing comprises and washes ammonia separation tower inlet end (13-1), wash ammonia separation tower first exit end (13-2) and wash ammonia separation tower second inlet end (13-3);
Described water cooler (12) comprises water cooler inlet end (12-1), water cooler first exit end (12-2) and water cooler second exit end (12-3);
The exit end of described raw gas compressor (1) is connected with the inlet end of oil eliminator (2); The exit end of oil eliminator (2) is connected with pre-thermal converter first inlet end (3-1); Pre-thermal converter first exit end (3-3) is connected with main thermal converter first inlet end (4-1); Main thermal converter first exit end (4-3) is connected with the inlet end of the first shift converter (7); First shift converter (7) is connected with main thermal converter second inlet end (4-2) by middle pressure waste-heat recoverer (6); Main thermal converter second exit end (4-4) is connected with the inlet end of separator (8); The exit end of separator (8) is connected with the inlet end of the second shift converter (9), and the second shift converter (9) is connected with pre-thermal converter second inlet end (3-2) by time middle pressure waste-heat recoverer (5); Pre-thermal converter second exit end (3-4) is connected with the inlet end of feedwater preheater (10); The exit end of feedwater preheater (10) is connected with the inlet end of de-salted water preheater (11); The exit end of de-salted water preheater (11) by water cooler (12) with wash ammonia separation tower inlet end (13-1) and be connected; Wash ammonia separation tower first exit end (13-2) to be connected with lime set interchanger (15) by stripping tower (14); The exit end of lime set interchanger (15) is connected with lime set water cooler inlet end (16-1); Lime set water cooler first exit end (16-2) is connected with water cooler second exit end (12-3); Lime set water cooler second exit end (16-3) with wash ammonia separation tower second inlet end (13-3) and be connected; Lime set water cooler the 3rd exit end (16-4) is connected with gasification cycle water pipe (17).
2. a kind of device for CO gas conversion and cooling according to claim 1, is characterized in that described oil eliminator (2) is provided with large by-pass, can purge when not stopping to it.
3. a kind of device for CO gas conversion and cooling according to claim 1, the conversion gas by-pass that it is characterized in that described pre-thermal converter (3) arranges the valve regulating coal gas.
4. a kind of device for CO gas conversion and cooling according to claim 1, the conversion gas by-pass that it is characterized in that described main thermal converter (4) arranges the valve regulating coal gas.
5. a kind of device for CO gas conversion and cooling according to claim 1, is characterized in that the pressure of described raw gas compressor (1) is 4.0MPaG.
6. a kind of device for CO gas conversion and cooling according to claim 1, is characterized in that described water cooler (12) is shell-and-tube fixed tube-sheet heat exchanger.
7. a kind of device for CO gas conversion and cooling according to claim 1, is characterized in that being provided with catalyst layer in described the first shift converter (7); Catalyzer in described catalyst layer is resistant to sulfur catalyst; Described resistant to sulfur catalyst contains 1.8%Co0 and 8.0%Mo0.
8. a kind of device for CO gas conversion and cooling according to claim 1, is characterized in that being provided with catalyst layer in described the second shift converter (9); Catalyzer in described catalyst layer is resistant to sulfur catalyst; Described resistant to sulfur catalyst contains 1.8%Co0 and 8.0%Mo0.
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| 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 |
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| CN201510128418.5A CN104828775B (en) | 2015-03-23 | 2015-03-23 | A device used for CO gas conversion and cooling |
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| CN104828775A true CN104828775A (en) | 2015-08-12 |
| CN104828775B CN104828775B (en) | 2017-02-08 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108862195A (en) * | 2018-06-19 | 2018-11-23 | 中国石油化工股份有限公司 | It is a kind of to improve the coal generating gas sulphur-resistant conversion system for stopping work cooling efficiency |
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| WO2010109107A1 (en) * | 2009-03-25 | 2010-09-30 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and equipment for producing hydrogen, using a thermokinetic compressor |
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| 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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2015
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Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US4161393A (en) * | 1977-03-07 | 1979-07-17 | Metallgesellschaft Aktiengesellschaft | Shift conversion of raw gas from gasification of coal |
| CN101157442A (en) * | 2007-04-27 | 2008-04-09 | 中国石化集团宁波工程有限公司 | Waste heat reclaiming process for CO transformation |
| CN101434379A (en) * | 2008-12-15 | 2009-05-20 | 四川天一科技股份有限公司 | Coke-oven gas transform processing method |
| WO2010109107A1 (en) * | 2009-03-25 | 2010-09-30 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and equipment for producing hydrogen, using a thermokinetic compressor |
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| 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 |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108862195A (en) * | 2018-06-19 | 2018-11-23 | 中国石油化工股份有限公司 | It is a kind of to improve the coal generating gas sulphur-resistant conversion system for stopping work cooling efficiency |
| 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 |
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