CN103881765B - Split circulating CO transformation process - Google Patents
Split circulating CO transformation process Download PDFInfo
- Publication number
- CN103881765B CN103881765B CN201410110655.4A CN201410110655A CN103881765B CN 103881765 B CN103881765 B CN 103881765B CN 201410110655 A CN201410110655 A CN 201410110655A CN 103881765 B CN103881765 B CN 103881765B
- Authority
- CN
- China
- Prior art keywords
- gas
- shift converter
- pressure
- temperature
- water
- 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.)
- Active
Links
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
Abstract
The invention relates to a split circulating CO transformation process, comprising the following steps: separating liquid from a crude synthesis gas of saturated steam conveyed from a pulverized coal gasification unit and preheating to certain temperature, and then entering a detoxification slot to remove impurities and heavy metal; then dividing the liquid without impurities and heavy metal into two strands, wherein the first strand of the liquid is mixed with high-pressure steam and a first strand of variable mixed gas and supplied to a medium-pressure boiler to supply water; entering a 1# shift converter to carry out shift reaction, and dividing the obtained variable mixed gas into two strands after heat exchange; entering a 2# shift converter to carry out shift reaction after mixing the second strand of variable mixed gas with the second strand of fresh synthesis gas; entering the obtained divalent mixed gas into a 3# shift converter to further carry out shift reaction after heat exchange. The CO concentration of the shift converter is effectively reduced by splitting the crude synthesis gas and the variable mixed gas, the operation temperature of the shift converter is low, the operation environment of the catalyst is mild, the stable operation cycle of the device is prolonged, and the energy conservation and consumption reduction effects are good.
Description
Technical field
The present invention relates to a kind of CO conversion process, specifically refer to a kind of share split circulation CO conversion process.
Background technology
China's Coal Gasification Technology achieves tremendous development in recent years, especially the powdered coal pressuring gasified technology of waste heat boiler flow process is adopted, have in, synthetic gas low to coal quality requirements that active principle is high, working cost is low and the features such as environmental friendliness, adopt 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 usually up to more than 60%, and water vapor volume content is less than 20% simultaneously, and crude synthesis gas has the distinguishing feature that vapour content is low and CO content is high.
The powdered coal pressuring gasified technology of waste heat boiler flow process is used for all needing configuration CO shift conversion step when gas making carrys out the devices such as supporting synthetic ammonia, hydrogen manufacturing, synthesizing methanol, regulates 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 produce the high concentration CO converter technique difficult problem that the product such as synthetic ammonia or methyl alcohol is all faced with strong heat release, so the popularization in recent years of the powdered coal pressuring gasified technology of waste heat boiler flow process and development, also promote 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, releases a large amount of reaction heat while generating carbonic acid gas and hydrogen.For the crude synthesis gas that different Coal Gasification Technology generates, 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.Fine coal for employing waste heat boiler flow process adds the crude synthesis gas that technology of calming the anger generates, when shift conversion step carries out CO transformationreation, how effectively the Focal point and difficult point of shift process design is the bed temperature of control CO transformationreation, extends the work-ing life of transformation catalyst and reduces transformationreation energy consumption.
Be matched in the shift process of this gasification technology at present, the more general sulfur resistant conversion process that have employed 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 becomes stove overtemperature in advance to prevent, hot steam is pressed through in the disposable interpolation of pre-transform stove entrance is a large amount of, the water in crude synthesis gas/dry gas mol ratio is made to reach more than 1.30, then transformationreation is carried out in segmentation, and final conversion gas outlet CO butt volume content is general not higher than 0.4%.
Existing high water-gas ratio CO shift process is in order to suppress the overtemperature of transformationreation, allocated into before crude synthesis gas enters pre-transform stove in a large number and press through hot steam, its water/dry gas mol ratio is made to reach 1.3 ~ 1.5, even if but like this, due to the thermopositive reaction that the CO concentration in crude synthesis gas is high and violent, still often there is pre-transform stove 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; Simultaneously due to need to allocate into more in press through hot steam, cause plant energy consumption high running cost large.
Summary of the invention
Technical problem to be solved by this invention provides a kind of share split circulation CO conversion process for the present situation of prior art, to solve the series of technical such as the catalyst life that the easy overtemperature of existing high water-gas ratio CO conversion process shift converter causes is short, energy consumption is high.
The present invention solves the problems of the technologies described above adopted technical scheme: this share split circulation CO conversion process, is characterized in that comprising the steps:
The crude synthesis gas temperature being saturated water vapor 155 DEG C ~ 165 DEG C sent here by coal gasification unit, pressure 3.65Mpa (G) ~ 3.75Mpa (G), water/dry gas mol ratio 0.18 ~ 0.19, CO butt volume content 60% ~ 70%, enter gas-liquid separator separates go out liquid laggard enter crude synthesis gas preheater preheats to temperature 215 DEG C ~ 225 DEG C, enter detoxification groove and remove impurity in crude synthesis gas and heavy metal;
The fresh synthesis gas going out detoxification groove is divided into two strands, the first strand of fresh synthesis gas wherein accounting for total amount 20% ~ 30v% with utilize the high pressure steam of high-pressure steam ejector injection temperature 535 DEG C ~ 540 DEG C, pressure 9.0Mpa (G) ~ 11.0Mpa (G) to produce first strand of 20% ~ 25v% that power sucks to become gas mixture and mix, then enter gas liquid mixer and the medium pressure boiler filled into feed water mix after enter 1# shift converter and carry out transformationreation; Control the mixture temperature 245 DEG C ~ 255 DEG C entering 1# shift converter, CO butt volume content 40% ~ 45%, water/dry gas mol ratio 1.3 ~ 1.5;
The conversion gas temperature going out 1# shift converter is 390 ~ 420 DEG C, CO butt volume content 2% ~ 4%, water/dry gas mol ratio 0.7 ~ 0.8; The change gas mixture going out 1# shift converter enters the useless pot output temperature 250 DEG C of pressure in 1#, the middle pressure saturation steam of pressure 4.0Mpa (G), fill in a change gas mixture after pressing saturation steam to mix in producing with pressing useless pot in the 2# of downstream, now a change mixture temperature is down to 270 DEG C ~ 290 DEG C, be divided into two strands, first strand one that wherein accounts for a change gas mixture total volumetric flow rate 20% ~ 25v% becomes gas mixture turns back to 1# shift converter entrance by high-pressure steam ejector suction; Remaining is enter 2# shift converter after second strand of one change gas mixture mixes with second strand of fresh synthesis gas to carry out transformationreation; The temperature of control 2# shift converter entrance gas mixture is 245 ~ 255 DEG C, CO butt volume content 38% ~ 45%, water/dry gas mol ratio is 0.75 ~ 0.85;
The two change mixture temperatures going out 2# shift converter are 420 ~ 435 DEG C, CO butt volume content 6% ~ 8%, water/dry gas mol ratio is 0.35 ~ 0.45; Enter the middle pressure saturation steam of the useless pot output temperature 250 DEG C of pressure in 2#, pressure 4.0Mpa (G), two change mixture temperatures are down to 260 ~ 270 DEG C simultaneously, after the heat exchange of crude synthesis gas preheater, temperature is down to 220 DEG C ~ 230 DEG C again, enter 3# shift converter and proceed transformationreation, the three change mixture temperatures going out 3# shift converter are 260 DEG C ~ 270 DEG C, CO butt volume content is 1% ~ 1.5%, water/dry gas mol ratio 0.25 ~ 0.35.Three change gas mixtures enter the temperature 130 DEG C that the preheating of oiler feed interchanger is sent here by battery limit (BL), the medium pressure boiler feedwater of pressure 5.0Mpa (G), by medium pressure boiler feed-water preheating to 200 DEG C, send downstream after three change mixture temperatures are down to 210 DEG C ~ 230 DEG C.
Compared with prior art, the invention has the advantages that:
1, circulate by utilizing vapo(u)r blasting to suck the lower concentration CO after converting, effectively reduce the CO concentration entering shift converter, reach shift converter service temperature and reduce, catalyzer running environment is gentle, catalyzer is elongated for work-ing life, and converter unit easily realizes the object of long-period stable operation;
2, in whole transformationreation process, only have the fresh crude synthesis gas of 20% ~ 30v% and component loops to return the one water/dry gas mol ratio become in gas mixture reaches 1.3 ~ 1.5, but the water-gas ratio of whole transformation system is lower all the time, in reducing, press through the consumption of hot steam.
3, the steam that converter unit is self-produced, all for the transformationreation of self, eliminates sect heat-exchanger and heat energy recovery equipment, simplifies technical process, save facility investment.
Accompanying drawing explanation
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 CO conversion process of the present embodiment supports the use the typical chemical fertilizer plant producing 300,000 tons/year of synthetic ammonia, 520,000 tons/year of urea in Shell Coal Gasification gas making.
As shown in Figure 1, this share split circulation CO conversion process comprises the steps:
The synthetic gas temperature being saturated water vapor 155 DEG C ~ 165 DEG C sent here by coal gasification unit, pressure 3.65Mpa (G) ~ 3.75Mpa (G), water/dry gas mol ratio 0.18 ~ 0.19, CO butt volume content 60% ~ 70%, due to calorific loss the process with pipeline raw gas being delivered to converter unit from gasification unit, a small amount of water vapour in synthetic gas can be condensed generation phlegma, synthetic gas and lime set coexist the corrosion and vibrations that can cause pipeline and equipment in tubing system, so synthetic gas needed lime set wherein to separate before entering pre-transform stove, therefore, synthetic gas is first sent into gas-liquid separator 1 by this example, isolated liquid is discharged from the bottom of gas-liquid separator 1.From gas-liquid separator 1 top, synthetic gas is out preheated to temperature 215 DEG C ~ 225 DEG C through synthesizer preheater 9, enters detoxification groove 2 and removes impurity in synthetic gas and heavy metal.The synthetic gas going out detoxification groove 2 is called fresh synthesis gas, and this gas is divided into two strands.Wherein first strand of fresh synthesis gas accounts for 20% ~ 30% of volume total amount, one of the volume total amount 20% ~ 25% that accounts for producing with utilizing the high pressure steam of high-pressure steam ejector 3 injection temperature 535 DEG C ~ 540 DEG C, pressure 9.0Mpa (G) ~ 11.0Mpa (G) that power sucks becomes gas mixture and mixes, then enter gas liquid mixer 4 to feed water with the medium pressure boiler filled into and mix, temperature and water-gas ratio are finely tuned.Control the mixture temperature 245 DEG C ~ 255 DEG C entering 1# shift converter 5, CO butt volume content 40% ~ 45%, water/dry gas mol ratio 1.3 ~ 1.5, enters 1# shift converter 5 and carries out depth conversion reaction.
After the reaction of 1# shift converter 5 depth conversion, the conversion gas temperature going out 1# shift converter 5 is about 390 ~ 420 DEG C, CO butt volume content 2% ~ 4%, water/dry gas mol ratio 0.7 ~ 0.8.One becomes gas mixture enters the useless pot 6 output temperature 250 DEG C of pressure in 1#, the middle pressure saturation steam of pressure 4.0Mpa (G), fill in a change gas mixture after pressing saturation steam to mix in producing with pressing useless pot 8 in the 2# of downstream, now a change mixture temperature is down to 270 DEG C ~ 290 DEG C, be divided into two strands, wherein one change gas mixture accounting for volume total amount 20% ~ 25% turns back to the entrance of 1# shift converter 5 by high-pressure steam ejector 3 suction; One accounts for one of volume total amount 75% ~ 80% and becomes gas mixture in addition, and the fresh synthesis gas accounting for fresh synthesis gas total amount 70% ~ 80% with second strand is infiltrated and carried out transformationreation into 2# shift converter 7.Wherein the temperature of 2# shift converter 7 entrance gas mixture is 245 ~ 255 DEG C, CO butt volume content 38% ~ 45%, and water/dry gas mol ratio is 0.75 ~ 0.85.
After the reaction of 2# shift converter 7 depth conversion, the two change mixture temperatures going out 2# shift converter 7 are 420 ~ 435 DEG C, CO butt volume content 6% ~ 8%, and water/dry gas mol ratio is 0.35 ~ 0.45.Enter the useless pot 8 output temperature 250 DEG C of pressure in 2#, the middle pressure saturation steam of pressure 4.0Mpa (G), two change mixture temperatures are down to 260 ~ 270 DEG C simultaneously, again after crude synthesis gas preheater 9 heat exchange temperature be down to ~ 230 DEG C, enter 3# shift converter 10 and proceed transformationreation, the three change mixture temperatures going out 3# shift converter 10 are 260 DEG C ~ 270 DEG C, and CO butt volume content is 1% ~ 1.5%, water/dry gas mol ratio 0.25 ~ 0.35.Three change gas mixtures enter the temperature 130 DEG C that oiler feed interchanger 11 preheating is sent here by battery limit (BL), the medium pressure boiler feedwater of pressure 5.0Mpa (G), by medium pressure boiler feed-water preheating to 200 DEG C, send downstream after three change mixture temperatures are down to 210 DEG C ~ 230 DEG C.
comparative example
China Petrochemical Industry's Anqing oil to gas project have employed the powdered coal pressuring gasified technology gas making of shell, for the production of 300,000 tons/year of synthetic ammonia, 520,000 tons/year of urea, have employed 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
* be supporting high water-gas ratio CO conversion process in Anqing oil to gas project 300,000 tons/year of synthetic ammonia 520,000 tons/year urine device.
* is the mixture of described first strand of fresh synthesis gas and described first strand of one change gas mixture.
Can be found out by table 1, share split circulation CO provided by the present invention converts new technology, effectively reduces the CO concentration entering shift converter, all plays 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 achieves and significantly reduces simultaneously, significant with reduction enterprise operation expense to the energy-conservation of converter unit.
Claims (1)
1. a share split circulation CO conversion process, is characterized in that comprising the steps:
The crude synthesis gas temperature being saturated water vapor 155 DEG C ~ 165 DEG C sent here by coal gasification unit, pressure 3.65Mpa (G) ~ 3.75Mpa (G), water/dry gas mol ratio 0.18 ~ 0.19, CO butt volume content 60% ~ 70%, enter and enter crude synthesis gas preheater (9) after liquid isolated by gas-liquid separator (1) and be preheated to temperature 215 DEG C ~ 225 DEG C, enter detoxification groove (2) and remove impurity in crude synthesis gas and heavy metal;
The fresh synthesis gas going out detoxification groove (2) is divided into two strands, the first strand of fresh synthesis gas wherein accounting for total amount 20% ~ 30% with utilize the high pressure steam of high-pressure steam ejector (3) injection temperature 535 DEG C ~ 540 DEG C, pressure 9.0Mpa (G) ~ 11.0Mpa (G) to produce power sucks 20% ~ 25% first strand one become gas mixture and mix, then enter gas liquid mixer (4) and the medium pressure boiler filled into feed water mix after enter 1# shift converter (5) and carry out transformationreation; Control enters the mixture temperature 245 DEG C ~ 255 DEG C of 1# shift converter (5), CO butt volume content 40% ~ 45%, water/dry gas mol ratio 1.3 ~ 1.5;
The conversion gas temperature going out 1# shift converter (5) is 390 ~ 420 DEG C, CO butt volume content 2% ~ 4%, water/dry gas mol ratio 0.7 ~ 0.8; The change gas mixture going out 1# shift converter (5) enters useless pot (6) the output temperature 250 DEG C of pressure in 1#, the middle pressure saturation steam of pressure 4.0Mpa (G), fill in a change gas mixture after mixing with the middle pressure saturation steam of pressing useless pot (8) to produce in the 2# of downstream, now a change mixture temperature is down to 270 DEG C ~ 290 DEG C, be divided into two strands, first strand one that wherein accounts for a change gas mixture total volumetric flow rate 20% ~ 25% becomes gas mixture turns back to 1# shift converter (5) entrance by high-pressure steam ejector (3) suction; Remaining is enter 2# shift converter (7) after second strand of one change gas mixture mixes with second strand of fresh synthesis gas to carry out transformationreation; The temperature of control 2# shift converter (7) entrance gas mixture is 245 ~ 255 DEG C, CO butt volume content 38% ~ 45%, water/dry gas mol ratio is 0.75 ~ 0.85;
The two change mixture temperatures going out 2# shift converter (7) are 420 ~ 435 DEG C, CO butt volume content 6% ~ 8%, water/dry gas mol ratio is 0.35 ~ 0.45; Enter the middle pressure saturation steam of useless pot (8) the output temperature 250 DEG C of pressure in 2#, pressure 4.0Mpa (G), two change mixture temperatures are down to 260 ~ 270 DEG C simultaneously, after crude synthesis gas preheater (9) heat exchange, temperature is down to 220 DEG C ~ 230 DEG C again, enter 3# shift converter (10) and proceed transformationreation, the three change mixture temperatures going out 3# shift converter (10) are 260 DEG C ~ 270 DEG C, CO butt volume content is 1% ~ 1.5%, water/dry gas mol ratio 0.25 ~ 0.35; Three change gas mixtures enter the temperature 130 DEG C that oiler feed interchanger (11) preheating is sent here by battery limit (BL), the medium pressure boiler feedwater of pressure 5.0Mpa (G), by medium pressure boiler feed-water preheating to 200 DEG C, after three change mixture temperatures are down to 210 DEG C ~ 230 DEG C, send downstream.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410110655.4A CN103881765B (en) | 2014-03-24 | 2014-03-24 | Split circulating CO transformation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410110655.4A CN103881765B (en) | 2014-03-24 | 2014-03-24 | Split circulating CO transformation process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103881765A CN103881765A (en) | 2014-06-25 |
| CN103881765B true CN103881765B (en) | 2015-07-08 |
Family
ID=50950904
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410110655.4A Active CN103881765B (en) | 2014-03-24 | 2014-03-24 | Split circulating CO transformation process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103881765B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104340958B (en) * | 2013-07-30 | 2016-09-07 | 航天长征化学工程股份有限公司 | high-CO raw gas conversion process obtained by pressure gasification of pulverized coal |
| CN104152187B (en) * | 2014-08-06 | 2016-02-17 | 中石化宁波工程有限公司 | A kind of can the CO conversion process in extending catalyst work-ing life |
| CN105905869B (en) * | 2016-04-14 | 2018-02-06 | 中石化南京工程有限公司 | A kind of coal hydrogen manufacturing CO converts Poly-generation method and device |
| CN110921621B (en) * | 2019-10-24 | 2023-04-07 | 中石化宁波工程有限公司 | Low-steam-ratio poly-generation isothermal transformation process and isothermal transformation furnace matched with pulverized coal gasification |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1443735A (en) * | 1972-09-08 | 1976-07-21 | Parsons Co Ralph M | Production of substitute natural gas |
| CN1069687C (en) * | 1998-07-03 | 2001-08-15 | 李群柱 | Process for purification to obtain high-purity synthetic gas by adsorption |
| CN1263864A (en) * | 2000-02-23 | 2000-08-23 | 刘洪文 | Process for synthesizing ammonia by partial transform of CO and low-temp. conversion |
| CN1204038C (en) * | 2001-12-30 | 2005-06-01 | 中国石化集团齐鲁石油化工公司 | CO isothermal sulfur resistant conversion process |
| CN100358851C (en) * | 2004-05-21 | 2008-01-02 | 庞玉学 | Method for producing methanol synthetic gas with hydrocarbon gas and coal as raw materials |
| CN100361889C (en) * | 2006-03-16 | 2008-01-16 | 五环科技股份有限公司 | Secondary transformation technological method of high concentration carbon monooxide |
| CN101704513B (en) * | 2009-08-13 | 2011-11-16 | 上海国际化建工程咨询公司 | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof |
| CN102002403B (en) * | 2010-11-09 | 2013-06-19 | 中国石油化工股份有限公司 | Low water-air ratio and middle water-air ratio carbon monoxide (CO) conversion process |
| CN102337160B (en) * | 2011-08-30 | 2013-09-18 | 中国石油化工股份有限公司 | High-water-steam-ratio saturated hot water tower split CO transformation process |
| CN102887480B (en) * | 2012-10-08 | 2014-06-04 | 中国石油化工集团公司 | CO shift technique by connecting isothermal shift and thermal insulation shift in series |
-
2014
- 2014-03-24 CN CN201410110655.4A patent/CN103881765B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN103881765A (en) | 2014-06-25 |
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 | |
| CN103881765B (en) | Split circulating CO transformation process | |
| CN104340958B (en) | high-CO raw gas conversion process obtained by pressure gasification of pulverized coal | |
| CN205035336U (en) | Resistant sulphur transform process systems of high concentration CO part | |
| CN104192798B (en) | Adiabatic-isothermal shift technique for high-concentration CO raw gas | |
| CN101096331A (en) | Method for integral production of liquid ammonia and methanol and/or dimethyl ether by using coke oven gas as raw material | |
| CN101955154A (en) | Isothermal conversion process method for high-concentration carbon monoxide conversion | |
| 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 | |
| CN102659076B (en) | Method for co-production of various chemical products from natural gas, coal and petroleum | |
| CN102337161B (en) | Low water-to-gas ratio serial saturation tower and hot water tower CO conversion process | |
| CN103879960B (en) | A kind of self-circulation CO conversion process | |
| CN109385313A (en) | A kind of raw gas washing process | |
| CN103881766B (en) | Chilling cyclic CO (carbon monoxide) transformation process | |
| CN103881767B (en) | Circulating CO shift process of saturation tower | |
| CN203545947U (en) | high-purity hydrogen production system, and synthetic ammonia system | |
| CN102041120B (en) | Method for generating synthetic natural gas | |
| 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 | |
| CN103881768B (en) | Cyclic CO (carbon monoxide) transformation process | |
| CN103449364A (en) | High-concentration CO sulfur tolerance shift technology and device fully using reaction heat | |
| CN201439492U (en) | Shunting isothermal sulphur-resisting conversion device | |
| CN102337162A (en) | Low-water-steam-ratio saturated hot water tower CO transformation process | |
| CN203768006U (en) | Energy-saving type circulating CO change device |
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 |