CN101530718A - Process for adsorbing and separating light hydrocarbon in F-T synthesis circulation gas by variable temperature and pressure - Google Patents
Process for adsorbing and separating light hydrocarbon in F-T synthesis circulation gas by variable temperature and pressure Download PDFInfo
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- CN101530718A CN101530718A CN200810085009A CN200810085009A CN101530718A CN 101530718 A CN101530718 A CN 101530718A CN 200810085009 A CN200810085009 A CN 200810085009A CN 200810085009 A CN200810085009 A CN 200810085009A CN 101530718 A CN101530718 A CN 101530718A
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Abstract
The invention discloses a process for adsorbing and separating light hydrocarbon in F-T synthesis circulation gas by variable temperature and pressure, comprising the following steps: the F-T synthesis gas firstly enters a water washing tower (6) and is contacted with the desalted water countercurrent flowing down from the tower top; the oxygen compounds (acid, alcohol and aldehydes) and higher hydrocarbons (hydrocarbons higher than C4) in the circulation gas are washed down. The circulation gas enters from the bottom of an adsorption tower (7); the hydrocarbons in the synthesis circulation gas is adsorbed by the adsorbent (active carbon mainly) in the adsorber; the purified circulation gas comes out of the top of the adsorption tower, is cooled by a circulation gas cooler (10), subsequently enters a buffer tank (11), is then stabilized and sent to decarbonization process; little purified synthesis gas is extracted out of the buffer tank by a temperature-reduction fan (12) to be used for reducing the temperature of the adsorption tower with the regeneration completed. After the adsorbent adsorbs in a saturated state, the generation process is turned to; under the action of the steam heating and negative pressure pumping of a vacuum pump (14), the hydrocarbons adsorbed in the adsorbent are resolved out of the adsorbent, then cooled by a hydrocarbon steam cooler (13) and then sent to an oil-washing workshop section so as to be recovered.
Description
Technical field
The present invention relates to ICL for Indirect Coal Liquefaction F-T synthetic cyclic gas kind lighter hydrocarbons and remove technology.
Background technology
Higher (the v%=24.09% of F-T synthetic cyclic gas hydrocarbon content, m%=29.3%), adopt hot potash decarbonization in the Shanxi coalification institute pilot-plant, lighter hydrocarbons cause the solution bubble after being entered liquid phase by the solution condensation in absorption process, solution can not be smoothly under overhead streams, caused and blocked the liquid flooding tower, decarbonization system can not normally be moved.Also adopt hot potash decarbonization in the industrialized unit of building now (Shanxi the Lushui River peace, Inner Mongol gouy Thailand), take place for fear of similar problem, this patent adopts the alternating temperature pressure swing adsorption that lighter hydrocarbons in the synthetic cyclic gas are removed, thereby eliminates the influence of lighter hydrocarbons to decarbonization system.Hydrocarbon removal process has solvent to absorb (being oil wash), cryogenic separation, film separation, transformation absorption in the existing gas.It is big that solvent absorbs investment, and operating cost height, degree of purification are low; The cryogenic separation degree of purification can guarantee, but its investment is big, energy consumption is high, operating cost is higher; Film separates because hydro carbons loses shortcomings such as big in film surface liquefaction problem and purified gas; Simple transformation absorption can not guarantee the regeneration effect of adsorbent.This patent adopts the synthetic hydro carbons that follows in the circulating air of alternating temperature adsorbing and removing F-T, and it is little to have an investment, and the automaticity height is easy and simple to handle, the advantage that degree of purification is high.
Summary of the invention
This patent adopts lighter hydrocarbons in the alternating temperature transformation adsorbing separation F-T synthetic cyclic gas, has solved in the F-T synthetic cyclic gas lighter hydrocarbons to the influence of back decarbonization process.
This patent adopts adsorption technology that lighter hydrocarbons in the synthetic cyclic gas are removed, thereby eliminates the influence of lighter hydrocarbons to decarbonization system.Because active carbon is to hydro carbons C particularly
4Above hydro carbons absorption affinity is stronger, adsorbs the regeneration degree that is difficult to guarantee adsorbent as simple employing transformation, and this patent alternating temperature pressure swing adsorption technique can guarantee the degree of purification that hydro carbons removes, and can also prolong the service life of adsorbent.
The technical scheme (as shown in drawings) that this patent technical solution problem is adopted:
Be introduced into desalted water counter current contacting under water scrubber (6) and the overhead streams in the F-synthetic cyclic gas, oxygenatedchemicals in the synthetic cyclic gas (acid, alcohol, aldehydes) and macromolecule hydrocarbon (C
4Above hydro carbons) is washed down.Circulating air enters from adsorption tower (7) bottom, hydro carbons is adsorbed adsorbent (mainly the being active carbon) absorption in the device in the synthetic cyclic gas, the circulating air that purified comes out to be sent to decarbonization process after entering surge tank (11) voltage stabilizing after recycle gas cooler (10) cooling from the adsorption tower top, purifies synthesis gas on a small quantity and is extracted out from surge tank in order to give the adsorption tower cooling usefulness of regeneration ending by temperature-dropping fan (12).After adsorbents adsorb is saturated, enter regenerative process, take out under the effect of negative pressure in Steam Heating and vavuum pump (14), the hydro carbons that is attracted in the adsorbent parses from adsorbent, is sent to oil wash workshop section and is reclaimed after hydrocarbon steam condenser (13) cooling.
Patent beneficial effect of the present invention is, adopts the absorption of alternating temperature transformation effectively lighter hydrocarbons in the F-T synthetic cyclic gas to be removed, thus eliminate hydro carbons in the synthetic cyclic gas to decarburization after the influence of system.Adopt the combination of alternating temperature, two kinds of renovation process of transformation, guaranteed to guarantee the adsorption effect of adsorbent, prolonged the service life of adsorbent, reduced the loss of hydro carbons.
Description of drawings
Accompanying drawing is a lighter hydrocarbons process chart in the alternating temperature transformation adsorbing separation F-T synthetic cyclic gas
Among the figure: 1 blowback cooling valve, 2 regeneration cooling valves, 3 circulating air outlet valves, 4 circulating air inlet valves, 5 hydrocarbon vapour outlet valves, 6 water scrubbers, 7 adsorption tower A, 8 adsorption tower B, 9 adsorption tower C, 10 recycle gas cooler, 11 surge tanks, 12 temperature-dropping fans, 13 hydrocarbon steam condensers, 14 vavuum pumps.
The specific embodiment
The technological process narration
The sorption cycle of each adsorption tower of this patent has absorption, regeneration, punching press, four steps of cooling, is that the concrete substep of example is set forth with adsorption tower (7) in the explanation accompanying drawing below.
1, adsorption process: synthetic cyclic gas enters water scrubber (6), and macromolecule hydrocarbon wherein and oxycompound are washed gets off to be sent to synthesizing section; The circulating air that comes out from the water scrubber top enters adsorption tower A (7) from the bottom, hydro carbons wherein is adsorbed agent (mainly being active carbon) absorption, the circulating air that purified comes out to be sent to decarbonization process after entering surge tank (11) voltage stabilizing after recycle gas cooler (10) cooling from the adsorption tower top, purifies synthesis gas on a small quantity and is extracted out from surge tank in order to give the adsorption tower cooling usefulness of regeneration ending by temperature-dropping fan (12).Treat the saturated back of adsorbent (methane content can be judged from exit gas), synthetic cyclic gas inlet valve (4) outlet valve (3) cuts out, and synthesis gas enters another tower absorption, and adsorption process finishes.
2, regenerative process: adsorption process finishes, adsorption tower regeneration steam valve (2), hydrocarbon steam outlet valve (5) are opened, the hydro carbons that is adsorbed desorbs from adsorbent under heating steam heat effect and vavuum pump (14) swabbing action, after hydrocarbon cooler (13) cooling, be sent to oil wash workshop section and the hydrogenation rich gas converges through the vavuum pump pressurization.During regeneration ending, regeneration steam valve (2), hydrocarbon steam outlet valve (5) are closed.
3, pressurising process: regenerative process finishes, the slow open valve of blowback cooling valve (valve 1) 10%, and the blowback air that comes from temperature-dropping fan (12) enters to the adsorption tower pressurising from adsorption tower A (7) bottom.
4, temperature-fall period: when the pressurising process finishes, blowback cooling valve (1) is opened to 100%, circulating air outlet valve (3) is opened simultaneously, temperature-fall period begins, when the adsorption tower temperature is identical with the blowback air temperature, blowback air cooling valve (1) is closed, and circulating air inlet valve (4) is opened the temperature-fall period end simultaneously, and adsorption tower enters next sorption cycle.
Claims (3)
1. lighter hydrocarbons technology in the alternating temperature adsorbing separation F-T synthetic cyclic gas is characterized in that, with the method for lighter hydrocarbons in the Activated Carbon Adsorption Separation F-T synthetic cyclic gas.
2. according to lighter hydrocarbons technology in the described alternating temperature adsorbing separation F-T synthetic cyclic gas of claim 1, it is characterized in that this method adsorbent reactivation adopts alternating temperature, voltage-transforming method.
3. according to lighter hydrocarbons technology in the described alternating temperature adsorbing separation F-T synthetic cyclic gas of claim 1, it is characterized in that this technology adsorption tower adopts the shell-and-tube adsorption tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810085009A CN101530718A (en) | 2008-03-13 | 2008-03-13 | Process for adsorbing and separating light hydrocarbon in F-T synthesis circulation gas by variable temperature and pressure |
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| Application Number | Priority Date | Filing Date | Title |
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| CN200810085009A CN101530718A (en) | 2008-03-13 | 2008-03-13 | Process for adsorbing and separating light hydrocarbon in F-T synthesis circulation gas by variable temperature and pressure |
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| CN101530718A true CN101530718A (en) | 2009-09-16 |
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| CN200810085009A Pending CN101530718A (en) | 2008-03-13 | 2008-03-13 | Process for adsorbing and separating light hydrocarbon in F-T synthesis circulation gas by variable temperature and pressure |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105935537A (en) * | 2016-04-19 | 2016-09-14 | 杨皓 | Process for purifying chlorosilane and hydrogen chloride with hydrogen mixed gas |
| CN107715648A (en) * | 2017-10-19 | 2018-02-23 | 泉州市天龙环境工程有限公司 | A kind of recovery system and its recovery process of toluene waste gas steam desorption |
| CN108367230A (en) * | 2016-03-08 | 2018-08-03 | 卡萨尔公司 | Temp.-changing adsorption method |
| CN114736722A (en) * | 2022-05-26 | 2022-07-12 | 上海科利蓝环境科技有限公司 | Coke oven gas adsorption purification and adsorbent regeneration treatment system and process |
| CN115491231A (en) * | 2022-10-21 | 2022-12-20 | 中国石油化工股份有限公司 | Isoparaffin solvent refining system and refining method |
| CN115537227A (en) * | 2022-10-21 | 2022-12-30 | 中国石油化工股份有限公司 | Adsorption tower and method for removing oxygen-containing compounds in isoparaffin solvent |
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2008
- 2008-03-13 CN CN200810085009A patent/CN101530718A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108367230A (en) * | 2016-03-08 | 2018-08-03 | 卡萨尔公司 | Temp.-changing adsorption method |
| US10874974B2 (en) | 2016-03-08 | 2020-12-29 | Casale Sa | Temperature-swing adsorption process |
| CN108367230B (en) * | 2016-03-08 | 2021-02-19 | 卡萨尔公司 | Temperature swing adsorption process |
| CN105935537A (en) * | 2016-04-19 | 2016-09-14 | 杨皓 | Process for purifying chlorosilane and hydrogen chloride with hydrogen mixed gas |
| CN105935537B (en) * | 2016-04-19 | 2018-10-02 | 杨皓 | A kind of technique of hydrogen mixed gas purified chlorosilane and hydrogen chloride |
| CN107715648A (en) * | 2017-10-19 | 2018-02-23 | 泉州市天龙环境工程有限公司 | A kind of recovery system and its recovery process of toluene waste gas steam desorption |
| CN114736722A (en) * | 2022-05-26 | 2022-07-12 | 上海科利蓝环境科技有限公司 | Coke oven gas adsorption purification and adsorbent regeneration treatment system and process |
| CN115491231A (en) * | 2022-10-21 | 2022-12-20 | 中国石油化工股份有限公司 | Isoparaffin solvent refining system and refining method |
| CN115537227A (en) * | 2022-10-21 | 2022-12-30 | 中国石油化工股份有限公司 | Adsorption tower and method for removing oxygen-containing compounds in isoparaffin solvent |
| CN115537227B (en) * | 2022-10-21 | 2024-06-21 | 中国石油化工股份有限公司 | Adsorption tower and method for removing oxygen-containing compound in isoparaffin solvent |
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Open date: 20090916 |