CN103881767A - Circulating CO shift process of saturation tower - Google Patents
Circulating CO shift process of saturation tower Download PDFInfo
- Publication number
- CN103881767A CN103881767A CN201410111811.9A CN201410111811A CN103881767A CN 103881767 A CN103881767 A CN 103881767A CN 201410111811 A CN201410111811 A CN 201410111811A CN 103881767 A CN103881767 A CN 103881767A
- Authority
- CN
- China
- Prior art keywords
- gas
- water
- shift
- strand
- saturator
- 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
Links
Images
Classifications
-
- 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
Landscapes
- Industrial Gases (AREA)
Abstract
The invention relates to a circulating CO shift process of a saturation tower. The circulating CO shift process comprises the following steps that a coarse synthetic gas from a pulverized coal gasification unit is divided into two branches, the first branch of coarse synthetic gas is moisturized and heated in the saturation tower and then mixed with high pressure steam and a first branch of primary shift gas and replenished with medium-pressure boiler water, and then the obtained mixture is fed into a No.1 shift furnace for shift reaction, the obtained primary shift gas is divided into two branches after heat exchange, the second branch of primary shift gas is mixed with the first branch of coarse synthetic gas to obtain a primary shift mixed gas, the primary shift mixed gas is mixed and replenished with medium-pressure steam and then fed into a No.2 shift furnace for continuous shift reaction, and the secondary shift gas is fed into a No.3 shift furnace for reaction after heat exchange. The operation of dividing the coarse synthetic gas and the primary shift gas into branches in the circulating CO shift process, so that the CO concentration entering the shift furnaces is effectively reduced; the operating temperatures of the shift furnaces are low, and the operating environment of a catalyst is mild, so that the service life of the catalyst and the operation period of the device are prolonged; and meanwhile, the amount of steam used is reduced, and the effects of energy conservation and consumption reduction are remarkable.
Description
Technical field
The present invention relates to CO conversion process, specifically refer to a kind of saturator circulation CO conversion process.
Background technology
China's Coal Gasification Technology has obtained tremendous development in recent years, especially adopt the powdered coal pressuring gasified technology of waste heat boiler flow process, have ature of coal is required in low, synthetic gas, active principle is high, working cost is low and the feature such as environmental friendliness, adopted by domestic increasing large-scale coal chemical engineering equipment.In the crude synthesis gas that the powdered coal pressuring gasified technology of waste heat boiler flow process generates, CO butt volume content is conventionally up to more than 60%, and water vapor volume content is less than 20% simultaneously, and crude synthesis gas has the low and high distinguishing feature of CO content of vapour content.
The powdered coal pressuring gasified technology of waste heat boiler flow process all needs to configure CO shift conversion step while carrying out the devices such as supporting synthetic ammonia, hydrogen manufacturing, synthesizing methanol for gas making, regulate the hydrogen-carbon ratio in synthetic gas maybe as far as possible many CO to be transformed to hydrogen by conversion.Therefore, no matter be the high concentration CO converter technique difficult problem that the products such as production synthetic ammonia or methyl alcohol are all faced with strong heat release, so popularization and the development in recent years of the powdered coal pressuring gasified technology of waste heat boiler flow process, has also promoted the development and progress of China's high concentration CO converter technique greatly.
Transformationreation is the reaction with same mole of water vapor and CO, emits a large amount of reaction heat when generating carbonic acid gas and hydrogen.The crude synthesis gas generating for different Coal Gasification Technology, the chemical reaction process of shift conversion step is all identical, but shift process need design targetedly according to the feature of crude synthesis gas.Add for the fine coal that adopts waste heat boiler flow process the crude synthesis gas that the technology of calming the anger generates, in the time that shift conversion step carries out CO transformationreation, the Focal point and difficult point of shift process design is bed temperature how effectively to control CO transformationreation, extends the work-ing life of transformation catalyst and reduces transformationreation energy consumption.
Be matched at present the shift process of this gasification technology, more general employing the sulfur resistant conversion process of high water-gas ratio, before shift conversion step is all arranged on crude synthesis gas desulfurization.Adopt high water-gas ratio sulfur resistant conversion process, its process features is to become in advance stove overtemperature in order to prevent, in the pre-disposable interpolation of shift converter entrance is a large amount of, press superheated vapour, water/dry gas mol ratio in crude synthesis gas is reached more than 1.30, then transformationreation is carried out in segmentation, and final conversion gas outlet CO butt volume content is not generally higher than 0.4%.
Existing high water-gas ratio CO shift process is in order to suppress the overtemperature of transformationreation, in allocating in a large number, press superheated vapour before crude synthesis gas enters pre-shift converter, make its water/dry gas mol ratio reach 1.3～1.5, even but like this, due to the high and violent thermopositive reaction of CO concentration in crude synthesis gas, still often there is pre-shift converter overtemperatute in device in operational process.Once overtemperature must cause pre-change catalyzer activity sharply to fail, catalyst change is frequent, affects the long-period stable operation of changing device; Owing to need to allocating more middle pressure superheated vapour into, cause the high running cost of plant energy consumption large simultaneously.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of saturator circulation CO conversion process for the present situation of prior art, with the series of technical such as solve the easy overtemperature of existing high water-gas ratio CO conversion process shift converter, catalyst life is short, energy consumption is high.
The present invention solves the problems of the technologies described above adopted technical scheme: this saturator circulation CO conversion process, is characterized in that comprising the steps:
155 DEG C～165 DEG C of the temperature, the pressure 3.65Mpa(G that are sent here by coal gasification unit)～3.75Mpa(G), the crude synthesis gas of water/dry gas mol ratio 0.18～0.19, CO butt volume content 60%～70% is divided into two strands, the volume ratio of first strand of crude synthesis gas and second strand of crude synthesis gas is 70～80:30～20;
First strand of crude synthesis gas enters saturator from the lower sidewall of saturator, and the temperature of sending here with the hot-water tower bottom entering from top is that the process recycled water counter current contact of 205 DEG C～215 DEG C is carried out heat and mass; Technological cycle water temp is reduced to 160 DEG C～170 DEG C and sends from saturator bottom, after saturated column bottoms pump pressurization, deliver to hot-water tower and carry out circulating-heating, extract 3%～8% of technological cycle water inventory simultaneously out and go rear system to carry out stripping, prevent that objectionable impurities from accumulating at technological cycle water system;
First strand of crude synthesis gas in saturator in humidification by temperature raising, temperature reaches 195 DEG C～205 DEG C, water/dry gas mol ratio reaches 0.80～0.90, first strand of crude synthesis gas after humidification temperature raising sent from saturator top;
Second strand of crude synthesis gas with utilize 535 DEG C～540 DEG C of high-pressure steam ejector injection temperatures, pressure 9.0Mpa(G)～11.0Mpa(G) and high pressure steam produce first strand of linear transformation gas that power sucks and mix, then enter gas liquid mixer and fill into and enter 1# shift converter after medium pressure boiler water and carry out transformationreation; Control enters 245 DEG C～255 DEG C of mixture temperatures, CO butt volume content 45%～50%, water/dry gas mol ratio 1.1～1.3 of 1# shift converter;
The linear transformation temperature degree that goes out 1# shift converter is 420 DEG C～430 DEG C, CO butt volume content 6.8%～7.8%, water/dry gas mol ratio 0.55～0.65, linear transformation gas enters the first preheater heating process recirculated water, and the temperature of linear transformation simultaneously degree is down to 370 DEG C～380 DEG C;
The linear transformation gas that goes out the first preheater is divided into two strands, and the throughput ratio of first strand of linear transformation gas and second strand of linear transformation gas is 15～20:80～85; Wherein first strand of linear transformation gas aspirates the entrance that turns back to 1# shift converter by high-pressure steam ejector; Second strand of linear transformation gas mixes with the first strand of crude synthesis gas going out after the humidification temperature raising of saturator, obtains a change gas mixture; Mixed one becomes 250 DEG C～260 DEG C of mixture temperatures, CO butt volume content 40%～45%, and water/dry gas mol ratio 0.70～0.80, fills into and enters 2# shift converter after middle pressure steam and proceed transformationreation; The change mixture temperature that control enters 2# shift converter is 245 DEG C～255 DEG C, water/dry gas mol ratio 0.80～0.90;
The quadratic transformation temperature degree that goes out 2# shift converter is that 430 DEG C～440 DEG C, CO butt volume content 6.0%～7.0%, water/dry gas mol ratio are 0.35～0.45;
Quadratic transformation gas enters the middle pressure saturation steam of 250 DEG C of the useless pot of middle pressure output temperature, pressure 4.0Mpa (G); Quadratic transformation temperature degree is down to 340 DEG C～350 DEG C, enters the second preheater heating process recirculated water, and quadratic transformation temperature degree is further reduced to 225 DEG C～235 DEG C, enters 3# shift converter and proceeds transformationreation;
The cubic transformation temperature degree that goes out 3# shift converter is that 265 DEG C～275 DEG C, CO butt volume content are 1%～1.5%, water/dry gas mol ratio 0.35～0.45;
Cubic transformation gas enters the 3rd preheater heating process recirculated water; Cubic transformation temperature degree is down to 170 DEG C～180 DEG C and is entered hot-water tower from bottom, carry out mass-and heat-transfer with the process recycled water counter current contact entering from middle part from saturator, then the top of hot-water tower with carry out countercurrent mass transfer heat transfer from the purification process phlegma of rear system and the medium pressure boiler water filling into, the ratio of purification process phlegma and medium pressure boiler quality is 1:1～1:2, cubic transformation temperature degree is reduced to 160～170 DEG C gradually, sends to downstream recovery waste heat from hot-water tower top; The technological cycle water temp of sending from hot-water tower bottom rises to 165 DEG C～175 DEG C, through the pressurization of hot water column bottoms pump and send saturator successively after the 3rd preheater, the second preheater and the first preheater stage-by-stage heat exchange to 205 DEG C～215 DEG C.
Compared with prior art, the invention has the advantages that:
1, use saturator to carry out warming and humidifying to crude synthesis gas, can save a large amount of middle superheated vapours of pressing, reduced significantly the steam consumption of converter unit;
2, circulate by the lower concentration CO that utilizes vapo(u)r blasting to suck after conversion, effectively reduce the CO concentration that enters shift converter, reached shift converter service temperature and reduced, catalyzer running environment gentleness, catalyzer is elongated work-ing life, and converter unit stable operation cycle is long;
3, in whole transformationreation process, mixed water/the dry gas of the linear transformation gas mol ratio that only has 25%～35% crude synthesis gas and partly loop back reaches 1.1～1.3, but the water-gas ratio of whole transformation system is lower all the time, reduce the consumption of middle pressure superheated vapour.
Brief description of the drawings
Fig. 1 is the process flow diagram of the embodiment of the present invention.
Embodiment
Below in conjunction with accompanying drawing embodiment, comparative example, the present invention is further elaborated.
Embodiment
The present embodiment is supported the use in Shell Coal Gasification gas making and produced on the typical chemical fertilizer plant of 520,000 tons/year of urea of 300,000 tons/year of synthetic ammonia.
As shown in Figure 1, this saturator circulation CO conversion process comprises the steps:
155 DEG C～165 DEG C of the temperature, the pressure 3.65Mpa(G that are sent here by coal gasification unit)～3.75Mpa(G), the crude synthesis gas of water/dry gas mol ratio 0.18～0.19, CO butt volume content 60%～70% is divided into two strands, the volume ratio of first strand of crude synthesis gas and second strand of crude synthesis gas is 70～80:30～20;
First strand of crude synthesis gas enters saturator 1 from the lower sidewall of saturator, and the temperature of sending here with hot-water tower 12 bottoms that enter from top is that the process recycled water counter current contact of 205 DEG C～215 DEG C is carried out heat and mass; Technological cycle water temp is reduced to 160 DEG C～170 DEG C and sends from saturator 1 bottom, after saturated column bottoms pump 2 pressurizations, deliver to hot-water tower 12 and carry out circulating-heating, extract 3%～8% of technological cycle water inventory simultaneously out and go rear system to carry out stripping, prevent that objectionable impurities from accumulating at technological cycle water system;
First strand of crude synthesis gas is by temperature raising in the interior humidification of saturator 1, and temperature reaches 195 DEG C～205 DEG C, and water/dry gas mol ratio reaches 0.80～0.90, and first strand of crude synthesis gas after humidification temperature raising sent from saturator 1 top;
Second strand of crude synthesis gas with utilize 535 DEG C～540 DEG C of high-pressure steam ejector 3 injection temperatures, pressure 9.0Mpa(G)～11.0Mpa(G) and high pressure steam produce first strand of linear transformation gas that power sucks and mix, then enter gas liquid mixer 4 and fill into and enter 1# shift converter 5 after medium pressure boiler water and carry out transformationreation; Control enters 245 DEG C～255 DEG C of mixture temperatures, CO butt volume content 45%～50%, water/dry gas mol ratio 1.1～1.3 of 1# shift converter 5;
The linear transformation temperature degree that goes out 1# shift converter 5 is 420 DEG C～430 DEG C, CO butt volume content 6.8%～7.8%, water/dry gas mol ratio 0.55～0.65, linear transformation gas enters the first preheater 6 heating process recirculated waters, and the temperature of linear transformation simultaneously degree is down to 370 DEG C～380 DEG C;
The linear transformation gas that goes out the first preheater 6 is divided into two strands, and the throughput ratio of first strand of linear transformation gas and second strand of linear transformation gas is 15～20:80～85; Wherein first strand of linear transformation gas aspirates by high-pressure steam ejector 3 entrance that turns back to 1# shift converter 5; Second strand of linear transformation gas mixes with the first strand of crude synthesis gas going out after the humidification temperature raising of saturator 1, obtains a change gas mixture; Mixed one becomes 250 DEG C～260 DEG C of mixture temperatures, CO butt volume content 40%～45%, and water/dry gas mol ratio 0.70～0.80, fills into and enters 2# shift converter 7 after middle pressure steam and proceed transformationreation; The change mixture temperature that control enters 2# shift converter 7 is 245 DEG C～255 DEG C, water/dry gas mol ratio 0.80～0.90;
The quadratic transformation temperature degree that goes out 2# shift converter 7 is that 430 DEG C～440 DEG C, CO butt volume content 6.0%～7.0%, water/dry gas mol ratio are 0.35～0.45;
Quadratic transformation gas enters the middle pressure saturation steam of 250 DEG C of 8 output temperature of the useless pot of middle pressure, pressure 4.0Mpa (G); Quadratic transformation temperature degree is down to 340 DEG C～350 DEG C, enters the second preheater 9 heating process recirculated waters, and quadratic transformation temperature degree is further reduced to 225 DEG C～235 DEG C, enters 3# shift converter 10 and proceeds transformationreation;
The cubic transformation temperature degree that goes out 3# shift converter 10 is that 265 DEG C～275 DEG C, CO butt volume content are 1%～1.5%, water/dry gas mol ratio 0.35～0.45;
Cubic transformation gas enters the 3rd preheater 11 heating process recirculated waters; Cubic transformation temperature degree is down to 170 DEG C～180 DEG C and is entered hot-water tower 12 from bottom, carry out mass-and heat-transfer with the process recycled water counter current contact entering from middle part from saturator 1, then the top of hot-water tower 12 with carry out countercurrent mass transfer heat transfer from the purification process phlegma of rear system and the medium pressure boiler water filling into, the ratio of purification process phlegma and medium pressure boiler quality is 1:1～1:2, cubic transformation temperature degree is reduced to 160～170 DEG C gradually, sends to downstream recovery waste heat from hot-water tower 12 tops; The technological cycle water temp of sending from hot-water tower 12 bottoms rises to 165 DEG C～175 DEG C, through hot water column bottoms pump 13 pressurization and send saturator 1 successively after the 3rd preheater 11, the second preheater 9 and the first preheater 6 stage-by-stage heat exchanges to 205 DEG C～215 DEG C.
comparative example
China Petrochemical Industry's Anqing oil changes gas project and has adopted the powdered coal pressuring gasified technology gas making of shell, for the production of 520,000 tons/year of urea of 300,000 tons/year of synthetic ammonia, adopted high water-gas ratio CO shift process, gasification unit send effective gas (H2+CO) of converter unit to be approximately 85000Nm
3/ h.The significant parameter of itself and above-described embodiment is contrasted, the results are shown in Table shown in 1.
Table 1
* change the high water-gas ratio CO conversion process in 520,000 tons/year of urine devices of 300,000 tons/year of synthetic ammonia of gas project for supporting at Anqing oil.
* is the mixture of described second strand of crude synthesis gas and described first strand of linear transformation gas.
Can find out by table 1, adopt saturator circulation CO conversion conversion new technology, effectively reduce the CO concentration that enters shift converter, all play good result to extending in the control of shift converter temperature, the optimization of catalyzer running environment and work-ing life; The steam consumption of whole transformation system also significantly reduces simultaneously, significant to the energy-conservation of converter unit and reduction enterprise operation expense.
Claims (1)
1. a saturator circulation CO conversion process, is characterized in that comprising the steps:
155 DEG C～165 DEG C of the temperature, the pressure 3.65Mpa(G that are sent here by coal gasification unit)～3.75Mpa(G), the crude synthesis gas of water/dry gas mol ratio 0.18～0.19, CO butt volume content 60%～70% is divided into two strands, the volume ratio of first strand of crude synthesis gas and second strand of crude synthesis gas is 70～80:30～20;
First strand of crude synthesis gas enters saturator (1) from the lower sidewall of saturator, and the temperature of sending here with the hot-water tower entering from top (12) bottom is that the process recycled water counter current contact of 205 DEG C～215 DEG C is carried out heat and mass; Technological cycle water temp is reduced to 160 DEG C～170 DEG C and sends from saturator (1) bottom, after saturated column bottoms pump (2) pressurization, deliver to hot-water tower (12) and carry out circulating-heating, extract 3%～8% of technological cycle water inventory simultaneously out and go rear system to carry out stripping, prevent that objectionable impurities from accumulating at technological cycle water system;
First strand of crude synthesis gas in saturator (1) in humidification by temperature raising, temperature reaches 195 DEG C～205 DEG C, water/dry gas mol ratio reaches 0.80～0.90, first strand of crude synthesis gas after humidification temperature raising sent from saturator (1) top;
Second strand of crude synthesis gas with utilize 535 DEG C～540 DEG C of high-pressure steam ejector (3) injection temperatures, pressure 9.0Mpa(G)～11.0Mpa(G) and high pressure steam produce first strand of linear transformation gas that power sucks and mix, then enter gas liquid mixer (4) and fill into and enter 1# shift converter (5) after medium pressure boiler water and carry out transformationreation; Control enters 245 DEG C～255 DEG C of mixture temperatures, CO butt volume content 45%～50%, water/dry gas mol ratio 1.1～1.3 of 1# shift converter (5);
The linear transformation temperature degree that goes out 1# shift converter (5) is 420 DEG C～430 DEG C, CO butt volume content 6.8%～7.8%, water/dry gas mol ratio 0.55～0.65, linear transformation gas enters the first preheater (6) heating process recirculated water, and the temperature of linear transformation simultaneously degree is down to 370 DEG C～380 DEG C;
The linear transformation gas that goes out the first preheater (6) is divided into two strands, and the throughput ratio of first strand of linear transformation gas and second strand of linear transformation gas is 15～20:80～85; Wherein first strand of linear transformation gas aspirates the entrance that turns back to 1# shift converter (5) by high-pressure steam ejector (3); Second strand of linear transformation gas mixes with the first strand of crude synthesis gas going out after the humidification temperature raising of saturator (1), obtains a change gas mixture; Mixed one becomes 250 DEG C～260 DEG C of mixture temperatures, CO butt volume content 40%～45%, and water/dry gas mol ratio 0.70～0.80, fills into and enters 2# shift converter (7) after middle pressure steam and proceed transformationreation; The change mixture temperature that control enters 2# shift converter (7) is 245 DEG C～255 DEG C, water/dry gas mol ratio 0.80～0.90;
The quadratic transformation temperature degree that goes out 2# shift converter (7) is that 430 DEG C～440 DEG C, CO butt volume content 6.0%～7.0%, water/dry gas mol ratio are 0.35～0.45;
Quadratic transformation gas enters the middle pressure saturation steam of 250 DEG C of (8) output temperature of the useless pot of middle pressure, pressure 4.0Mpa (G); Quadratic transformation temperature degree is down to 340 DEG C～350 DEG C, enters the second preheater (9) heating process recirculated water, and quadratic transformation temperature degree is further reduced to 225 DEG C～235 DEG C, enters 3# shift converter (10) and proceeds transformationreation;
The cubic transformation temperature degree that goes out 3# shift converter (10) is that 265 DEG C～275 DEG C, CO butt volume content are 1%～1.5%, water/dry gas mol ratio 0.35～0.45;
Cubic transformation gas enters the 3rd preheater (11) heating process recirculated water; Cubic transformation temperature degree is down to 170 DEG C～180 DEG C and is entered hot-water tower (12) from bottom, carry out mass-and heat-transfer with the process recycled water counter current contact entering from middle part from saturator (1), then the top of hot-water tower (12) with carry out countercurrent mass transfer heat transfer from the purification process phlegma of rear system and the medium pressure boiler water filling into, the ratio of purification process phlegma and medium pressure boiler quality is 1:1～1:2, cubic transformation temperature degree is reduced to 165 DEG C gradually, sends to downstream recovery waste heat from hot-water tower (12) top; The technological cycle water temp of sending from hot-water tower (12) bottom rises to 165 DEG C～175 DEG C, through hot water column bottoms pump (13) pressurization and send saturator (1) successively after the 3rd preheater (11), the second preheater (9) and the first preheater (6) stage-by-stage heat exchange to 205 DEG C～215 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410111811.9A CN103881767B (en) | 2014-03-24 | 2014-03-24 | Circulating CO shift process of saturation tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410111811.9A CN103881767B (en) | 2014-03-24 | 2014-03-24 | Circulating CO shift process of saturation tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103881767A true CN103881767A (en) | 2014-06-25 |
| CN103881767B CN103881767B (en) | 2015-05-13 |
Family
ID=50950906
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410111811.9A Active CN103881767B (en) | 2014-03-24 | 2014-03-24 | Circulating CO shift process of saturation tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103881767B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109319733A (en) * | 2018-09-30 | 2019-02-12 | 中石化宁波工程有限公司 | The CO conversion process of mating methanol-fueled CLC |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5358696A (en) * | 1993-12-01 | 1994-10-25 | Texaco Inc. | Production of H2 -rich gas |
| CN102337161A (en) * | 2011-08-30 | 2012-02-01 | 中国石油化工股份有限公司 | Low water-to-gas ratio serial saturation tower and hot water tower CO conversion process |
| CN102337159A (en) * | 2011-08-30 | 2012-02-01 | 中国石油化工股份有限公司 | Saturated hot water tower high-water-steam-ratio CO transformation process |
| CN102701149A (en) * | 2012-06-07 | 2012-10-03 | 王揽月 | Water heat-transfer shift process for by-product high-grade steam energy-saving deep conversion |
| CN102888252A (en) * | 2012-10-08 | 2013-01-23 | 中国石油化工集团公司 | Saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology |
| CN102888253A (en) * | 2012-10-08 | 2013-01-23 | 中国石油化工集团公司 | Low-moisture low-variable serial saturation tower thermal CO transformation technology |
-
2014
- 2014-03-24 CN CN201410111811.9A patent/CN103881767B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5358696A (en) * | 1993-12-01 | 1994-10-25 | Texaco Inc. | Production of H2 -rich gas |
| CN102337161A (en) * | 2011-08-30 | 2012-02-01 | 中国石油化工股份有限公司 | Low water-to-gas ratio serial saturation tower and hot water tower CO conversion process |
| CN102337159A (en) * | 2011-08-30 | 2012-02-01 | 中国石油化工股份有限公司 | Saturated hot water tower high-water-steam-ratio CO transformation process |
| CN102701149A (en) * | 2012-06-07 | 2012-10-03 | 王揽月 | Water heat-transfer shift process for by-product high-grade steam energy-saving deep conversion |
| CN102888252A (en) * | 2012-10-08 | 2013-01-23 | 中国石油化工集团公司 | Saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology |
| CN102888253A (en) * | 2012-10-08 | 2013-01-23 | 中国石油化工集团公司 | Low-moisture low-variable serial saturation tower thermal CO transformation technology |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109319733A (en) * | 2018-09-30 | 2019-02-12 | 中石化宁波工程有限公司 | The CO conversion process of mating methanol-fueled CLC |
| CN109319733B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | CO conversion process matched with methanol synthesis |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103881767B (en) | 2015-05-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101704513B (en) | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof | |
| CN102002403B (en) | Low water-air ratio and middle water-air ratio carbon monoxide (CO) conversion process | |
| CN104340958B (en) | high-CO raw gas conversion process obtained by pressure gasification of pulverized coal | |
| CN104192798B (en) | Adiabatic-isothermal shift technique for high-concentration CO raw gas | |
| CN103695058B (en) | Novel methanation reaction process for preparing synthetic natural gas | |
| CN104774663B (en) | One-step method coal synthetic natural gas and its system | |
| CN103449365B (en) | Process for converting high-concentration CO-tolerant sulfur and device thereof | |
| CN102337160B (en) | High-water-steam-ratio saturated hot water tower split CO transformation process | |
| CN102337159B (en) | Saturated hot water tower high-water-steam-ratio CO transformation process | |
| CN103881765B (en) | Split circulating CO transformation process | |
| CN102337161B (en) | Low water-to-gas ratio serial saturation tower and hot water tower CO conversion process | |
| CN103881767B (en) | Circulating CO shift process of saturation tower | |
| CN103879960B (en) | A kind of self-circulation CO conversion process | |
| CN103881766B (en) | Chilling cyclic CO (carbon monoxide) transformation process | |
| CN103449364B (en) | A kind of process for converting high-concentration CO-tolerant sulfur and device making full use of reaction heat | |
| CN102337162B (en) | Low-water-steam-ratio saturated hot water tower CO transformation process | |
| CN103879961B (en) | A kind of saturator share split circulation CO conversion process | |
| CN104058368A (en) | Process and system for producing hydrogen by converting hydrocarbon-containing tail gas | |
| CN204569865U (en) | Single stage method coal synthetic natural gas system | |
| CN202898012U (en) | High-concentration CO sulfur-tolerance conversion device sufficiently utilizing reaction heat | |
| CN201439492U (en) | Shunting isothermal sulphur-resisting conversion device | |
| CN203768006U (en) | Energy-saving type circulating CO change device | |
| CN203170305U (en) | Combined-heat-exchange multi-shell-side fixed bed production equipment for preparing olefin from methanol | |
| CN203768005U (en) | Overtemperature circulation preventing CO conversion device | |
| CN105505432A (en) | Comprehensive heat utilization method in methanol to gasoline process |
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 |