CN103058295B - Technology of low pressure steam stripping shift conversion technical condensed fluid - Google Patents
Technology of low pressure steam stripping shift conversion technical condensed fluid Download PDFInfo
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- CN103058295B CN103058295B CN201210553632.1A CN201210553632A CN103058295B CN 103058295 B CN103058295 B CN 103058295B CN 201210553632 A CN201210553632 A CN 201210553632A CN 103058295 B CN103058295 B CN 103058295B
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Abstract
The invention relates to technology of low pressure steam stripping shift conversion technical condensed fluid, which solves the problem existing in the existing technology of steam stripping shift conversion technical condensed fluid that equipment and pipelines are blocked and eroded and stable running of a shift conversion unit is badly influenced. The technical scheme comprises the following steps: feeding process condensate to the upper part of a condensate stripping tower so as to be contacted with low-pressure steam in backward flow; carrying out steam stripping; carrying out steam stripping on NH3 and CO2 in the converted process condensate; controlling the pressure of the steam stripping to be 0.1 MpaG to 0.2 MpaG; cooling tail gas after steam stripping at the top of the tower after steam stripping till the temperature of 85-110 DEG C; and then entering a tail gas separator. The technology is simple in process, simple and convenient to operate, can efficiently solve the problems of crystallization of ammonium bicarbonate and thiamine on steam stripping gas processing pipelines, equipment blockage and corrosion while ammonia and carbon dioxide in the process condensate can be extracted, and ensures stable running of the shift conversion unit.
Description
Technical field
The present invention relates to a kind of technique of stripping conversion process phlegma, specifically a kind of technique of low pressure stripping conversion process phlegma.
Background technology
Carbon monodixe conversion production technique is the key link in Coal Chemical Industry production process, is a kind of important purification process process in the techniques such as synthetic ammonia, methyl alcohol and hydrogen manufacturing.Adopt in the technical process of coal water slurry gasification explained hereafter synthetic gas, gasification enters in the raw gas of shift conversion step and contains a large amount of water vapors, and these water vapors, except subparticipation transformationreation, become after major part is cooled and need the process condensate got rid of.Adopting in the shell of dried coal powder gasification, GSP flow process, because water to steam ratio in raw gas is lower, need to supplement a part of steam to adjust water to steam ratio, therefore the quantity discharged of phlegma is less.For meeting water saving, energy-conservation requirement, the process condensate of coal water slurry flow process and dry powder flow process all will reclaim use.
Conversion process phlegma stripping is the significant process of conversion process Condensate reuse, and Main Function is by the CO being dissolved in conversion phlegma
2, the stripping such as ammonia out, avoid the accumulation of ammonia in system, cause equipment corrosion and system jams.The steam stripped effect of conversion phlegma directly affects the steady running of changing device.
Existing conversion phlegma stripping system, approximately 180 ℃～40 ℃ of service temperatures, working pressure is 0.35MpaG～0.8MpaG, stripping gas is water saturation state, to carbon steel CO
2seriously corroded also should be considered wet hydrogen sulfide damage simultaneously, should consider sulphide stress corrosion, chloride stress cracking corrosion to stainless steel.At present, all there is successively etching problem in the water cooler after being sent by phlegma stripping tower top stripping gas in some projects and follow-up pipeline and equipment thereof.
Existing phlegma steam stripping technique generally, from changing stripping process flow process, adopts the modes such as multitower stripping or multiply charging, and does not address the existing problem of phlegma stripping from operating parameters aspect.Phlegma stripping temperature, pressure are strictly controlled, or cannot strictly be controlled operating pressure and temperature, cause from stripping CO out
2, NH
3in subsequent condensation process, very easily form ammonium salt crystallization thing, cause obstruction and the corrosion of equipment, pipeline, have a strong impact on the steady running of converter unit.
If the patent No. is the Chinese invention patent disclosed " gas stripping process of process condensate in a kind of CO conversion " of ZL 200910098944.6, in order to solve conversion process phlegma stripping system generation ammonium salt crystallization blockage problem, adopt two stripping towers respectively to CO
2and NH
3carry out stripping, avoided CO
2and NH
3simultaneous possibility in system, has extended the cycle of changing device steady running, but it does not fundamentally solve the problem of pipeline, equipment obstruction and corrosion, and there are the following problems:
1) send the stripping gas temperature of torch low, easily cause the crystallization in stripping gas processing pipeline of carbon ammonium and thiamines, equipment stops up and etching problem fails to solve.
2) two tower flow processs, equipment is many, and operating system complexity need to be controlled respectively the working pressure of Shang Ta and lower tower and controls the secondary distribution amount of stripped vapor and take out ammonia amount, the pressure surge of a tower will cause another pressure tower also to fluctuate, and easily cause the unstable of operating pressure.Therefore, secondary distribution amount and to take out ammonia parameter control ratio more difficult, operation stability is waited to investigate.
Summary of the invention
The object of the invention is in order to solve the problems of the technologies described above, provide a kind of technique simple, easy and simple to handle, can extraction process can also effectively solve carbon ammonium and the crystallization of thiamines in stripping gas processing pipeline when ammonia and carbonic acid gas in phlegma, equipment stops up and etching problem.
Technical scheme comprises sends process condensate into phlegma stripping tower top, with low-pressure steam counter current contact, carries out steam stripped, by the NH in conversion process phlegma
3, CO
2stripping out, is controlled steam stripped pressure at 0.1MpaG～0.2MpaG, and after stripping, top of tower stripping tail gas out enters Reconstruction of End Gas Separator after being cooled to 85 ℃～110 ℃.
After described stripping, top of tower stripping tail gas is out cooled to 85 ℃～110 ℃ by air cooler.
Stripping tail gas is isolated phlegma and tail gas through Reconstruction of End Gas Separator, and tail gas is discharged through tower top, and phlegma is back to phlegma stripping tower top at the bottom of tower.
Contriver furthers investigate stripping pressure, and by the mesolow stripping Pressure Drop in past, to low pressure, i.e. 0.1MpaG～0.2MpaG, considers employing single tower process, CO
2and NH
3in same tower, extract, for suppressing the carrying out of crystallization reaction, step-down is more effective way, repeatedly studies through contriver, can guarantee that at the pressure of 0.1MpaG～0.2MpaG Srteam Stripping effect can farthest suppress again reaction and the generation of follow-up amine.
Further, contriver finds in research and development, and service temperature makes a strong impact to crystallization, and the crystallization of system mainly concentrates on stripping tail gas and goes out on tower rear line and equipment, goes out in the stripping tail gas of lowering the temperature after tower and contains a large amount of CO
2and NH
3if temperature is down to too low, very easily there is amine salt crystallisation problems, therefore must strictly control its temperature to the cooling of stripping tail gas, be cooled to 85 ℃～110 ℃, if very easily produce obstruction and the corrosion that a large amount of crystallizations causes pipeline and equipment lower than 85 ℃, if higher than 110 ℃ in air lift tail gas water-content increase, be unfavorable for that follow-up system processes tail gas.
The condensation of described stripping tail gas is preferably used air cooler.Preferred steam stripped temperature is controlled at 120～134 ℃, NH in process condensate after control stripping
3content is in 10～50ppm(molecular fraction).
Beneficial effect:
1. adopt low low-pressure steam formulation, utilize existing single tower process, change the mode of thinking, by the stripping pressure of Controlling System and the condensing temperature of stripping gas, by CO in conversion process phlegma
2and NH
3stripping out, effectively reduces the NH of transformation system simultaneously
3assemble, in the situation that not changing existing vaporizing extract process equipment, solved existing carbon monoxide conversion device seriously corroded, and the problem of the equipment of phlegma stripping operation, pipeline obstruction and corrosion.
2. adopt single tower flow process, technical process is simple, equipment is few, invests lowly, and Controlling System is simple, simple to operate, stable, Srteam Stripping effect is obvious, through trying three annual transform devices and stripper plant out, corrosion phenomenon does not all occur, greatly extend the work-ing life of equipment, guaranteed the steady running of converter unit.
3. be all recycled to phlegma stripping tower top through the isolated phlegma of Reconstruction of End Gas Separator and proceed stripping, realize the recovery of whole process condensates.
Accompanying drawing explanation
Fig. 1 is schema of the present invention.
Wherein, 1-phlegma stripping tower, 2-condenser, 3-air cooler, 4-Reconstruction of End Gas Separator, 5-force (forcing) pump, 6-reflux pump.
Embodiment
Below in conjunction with accompanying drawing, technique of the present invention is described further.
Embodiment 1:
The conversion process phlegma (hereinafter to be referred as phlegma) that changing device comes consists of (molecular fraction): H
2: 191ppm; CH
4: 23ppb; N
2: 2ppm; CO:56ppm; CO
2: 0.19%mol; NH
3: 386ppm, H
2s:62ppm, H
2o:99.74.Temperature: 125 ℃; Pressure: 2.8MpaG; Flow: 159855kg/h.
The process condensate that carrys out transformation into itself enters phlegma stripping tower 1 top, with the low-pressure steam counter current contact from pipe network, carries out steam stripped, by the CO in conversion process phlegma
2and NH
3out, control stripping pressure is 0.1MpaG to stripping, and stripping temperature is 120 ℃.From the stripping out of phlegma stripping tower 1 bottom, process condensate is cooled to 40 ℃, NH in condenser 2
3content is controlled at 20ppm, send downstream unit through force (forcing) pump 5; Air cooler 3, be cooled to 90 ℃ of laggard Reconstruction of End Gas Separators 4 from phlegma stripping tower 1 top stripping tail gas out, the phlegma that Reconstruction of End Gas Separator 4 is separated is transmitted back to phlegma stripping tower 1 top as phegma through reflux pump 6, and the stripping tail gas that goes out Reconstruction of End Gas Separator 4 send the processing of tail gas incinerator.
Embodiment 2:
The conversion process phlegma (hereinafter to be referred as phlegma) that changing device comes consists of (molecular fraction): H
2: 191ppm; N
2: 2ppm; CO:56ppm; CO
2: 387ppm; NH
3: 500ppm, H
2s:12ppm, H
2o:99.9.Temperature: 155 ℃; Pressure: 0.6MpaG; Flow: 45753kg/h.
The process condensate that carrys out transformation into itself enters phlegma stripping tower 1 top, with the low-pressure steam counter current contact from pipe network, carries out steam stripped, by the CO in conversion process phlegma
2and NH
3out, control stripping pressure is 0.2MpaG to stripping, and stripping temperature is 134 ℃.From the stripping out of phlegma stripping tower 1 bottom, process condensate is cooled to 40 ℃, NH in condenser 2
3content is controlled at 50ppm, send downstream unit through force (forcing) pump 5; Air cooler 3, be cooled to 110 ℃ of laggard Reconstruction of End Gas Separators 4 from phlegma stripping tower 1 top stripping tail gas out, the phlegma that Reconstruction of End Gas Separator 4 is separated is transmitted back to phlegma stripping tower 1 top as phegma through reflux pump 6, and the stripping tail gas that goes out Reconstruction of End Gas Separator 4 send the processing of tail gas incinerator.
The conversion process phlegma (hereinafter to be referred as phlegma) that changing device comes consists of (molecular fraction): H
2: 212ppm; N
2: 19ppm; CO:6ppm; CO
2: 0.2; NH
3: 800ppm, H
2s:56ppm, H
2o:99.7.Temperature: 78 ℃; Pressure: 1.1MpaG; Flow: 77820kg/h.
The process condensate that carrys out transformation into itself enters phlegma stripping tower 1 top, with the low-pressure steam counter current contact from pipe network, carries out steam stripped, by the CO in conversion process phlegma
2and NH
3out, control stripping pressure is 0.15MpaG to stripping, and stripping temperature is 127 ℃.From the stripping out of phlegma stripping tower 1 bottom, process condensate is cooled to 50 ℃, NH in condenser 2
3content is controlled at 30ppm, send downstream unit through force (forcing) pump 5; Air cooler 3, be cooled to 85 ℃ of laggard Reconstruction of End Gas Separators 4 from phlegma stripping tower 1 top stripping tail gas out, the phlegma that Reconstruction of End Gas Separator 4 is separated is transmitted back to phlegma stripping tower 1 top as phegma through reflux pump 6, and the stripping tail gas that goes out Reconstruction of End Gas Separator 4 send the processing of tail gas incinerator.
Claims (2)
1. a technique for low pressure stripping conversion process phlegma, comprises process condensate is sent into phlegma stripping tower top, with low-pressure steam counter current contact, carries out steam stripped, by the NH in conversion process phlegma
3, CO
2stripping out, is characterized in that, controls steam stripped pressure at 0.1MpaG～0.15MpaG, and after stripping, top of tower stripping tail gas out enters Reconstruction of End Gas Separator after air cooler is cooled to 85 ℃～90 ℃.
2. the technique of low pressure stripping conversion process phlegma as claimed in claim 1 or 2, is characterized in that, stripping tail gas is isolated phlegma and tail gas through Reconstruction of End Gas Separator, and tail gas is discharged through tower top, and phlegma is back to phlegma stripping tower top at the bottom of tower.
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| CN104208890B (en) * | 2013-05-30 | 2016-03-23 | 神华集团有限责任公司 | Stripping system and gas stripping process |
| CN103408084B (en) * | 2013-08-15 | 2016-03-09 | 中国寰球工程公司 | Single tower of built-in graphite condenser full blows out technique lime set stripping process |
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| CN104556148A (en) * | 2014-12-29 | 2015-04-29 | 安徽淮化股份有限公司 | Synthesis ammonia conversion condensate recycling treatment method and device thereof |
| CN109381887B (en) * | 2017-08-03 | 2021-10-08 | 中国石油化工股份有限公司 | Pretreatment system and method for high ammonia nitrogen acidic condensate of conversion unit |
| CN108147429A (en) * | 2018-02-12 | 2018-06-12 | 北京阳华科技有限公司 | A kind of gasification process that ammonia is carried for conversion section low temperature cold lime set |
| CN108383139B (en) * | 2018-04-20 | 2019-11-15 | 包头市远达鑫化工有限公司 | The process units and method of ammonium hydrogen carbonate |
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| CN102225819A (en) * | 2011-04-26 | 2011-10-26 | 中国石油化工股份有限公司 | Acidic water treatment method |
| CN102502901A (en) * | 2011-09-23 | 2012-06-20 | 中国石油化工股份有限公司 | Condensed fluid stripping method matched with CO transforming device |
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2012
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Patent Citations (7)
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| US4240808A (en) * | 1977-10-03 | 1980-12-23 | Metallgesellschaft Aktiengesellschaft | Processing aqueous effluent liquors from degasification or gasification of coal |
| US4260462A (en) * | 1978-05-26 | 1981-04-07 | United States Steel Corporation | Process for separating acid gases and ammonia from dilute aqueous solutions thereof |
| CN101597092A (en) * | 2009-01-09 | 2009-12-09 | 华南理工大学 | Single tower alkali injection pressurization stripping is handled the method for coal gasification wastewater |
| CN101570350A (en) * | 2009-05-22 | 2009-11-04 | 中国石油化工集团公司 | Steam stripping method of process condensate in CO conversion |
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