CN1817410A - Complete equipment for decreasing push, increasing pressure and desulfurizing and desulfurization thereof - Google Patents
Complete equipment for decreasing push, increasing pressure and desulfurizing and desulfurization thereof Download PDFInfo
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Abstract
A complete set of pressurizing and desulfurizing equipment for the top of pressure reducing tower to remove the H2S from its tail gas containing S is composed of pressurizing jet unit, solution tank, circulating pump unit, rich liquid pump unit, and cooler unit. Its desulfurizing technology features that the solution of methyl diethanolamine [(CH3)N(CH2CH2OH)2] is used as desulfurizing agent. Its advantages are high desulfurizing efficiency, simple structure and low cost.
Description
Technical Field
The invention relates to desulfurization equipment and a process thereof, in particular to complete equipment for top-reducing and pressurizing desulfurization and a desulfurization process thereof, which are used for removing H in high-sulfur top-reducing tail gas of an oil refinery2S。
Background
The 21 st century is a century of sustainable development, and as an environment-friendly work of important contents of sustainable development, the 21 st century becomes a focus of attention of people in the new century, and the environment protection is not only related to the quality of life of people, but also related to the survival and development of human beings. SO in industrial gases2And H2S is the main cause of acid rain pollution, and the effective method is to control the industrial gas desulfurizationThe content of the sulfur is given enough attention by the government of China, a plurality of autonomous technical challenges are developed, a large number of industrial gas desulfurization devices in developed countries are introduced, and a plurality of technical cooperation researches are developed with the developed countries, but the investment of the prior art is large and the cost is high. The contradiction between energy and environment in China needs to be solved properly, China cannot walk the old road of developed countries which is treated after pollution, and China must search for an energy environmental protection technology suitable for the national conditions. China carries out long-term work in the field of flue gas desulfurization, and how to research and develop a desulfurization technology suitable for different industrial production devices becomes an important task for scientific and technical personnel in China.
Many foreign research institutes and companies are researching the desulfurization technologyof industrial gas, and different desulfurization technologies are proposed according to different production devices. For example, Almatis developed a Claus Sulfur recovery catalyst, a proprietary SO of the CANSOLV technology corporation2A recovery process, a sulfur recovery technology of Fluor, a COPE and D' GAASS process of GAA, an LO-CAT process of GTP, a WSA process of Haldu-TopuSol, a DynaWave scrubber of Mengdoun environmental chemical systems, a Shell-Paques process of Shell, an ADIP process, a Claus process, a SCOT tail gas treatment process, a sulfur degassing process, a HIGHSULF process of TKK, and the like. Currently, over 200 gas desulfurization technologies are estimated for research, development and commercial application in various countries around the world. Gas desulfurization can be classified into a discard method and a regeneration recovery method according to whether or not a desulfurization product is recovered, wherein the desulfurization mixture is directly discharged, and the desulfurization by-product is recovered in the form of sulfuric acid or sulfur.
The existing gas desulfurization technology in China mainly depends on import, and the wet desulfurization technology has absolute advantages in the flue gas desulfurization technology which is successfully operated at home and abroad at present. In high sulfur containing gases, sulfur removal and recovery techniques have almost relied on importation. At present, the research on the aspect in China is in the beginning stage, and how to select a reasonable desulfurizer and reduce the secondary pollution of the desulfurizer is an important subject of the research on the desulfurization technology.
Along with the development of the domestic oil refining industry and the continuous expansion and new construction of oil refining devices, the demand for foreign crude oil is increasing, the quantity of imported crude oil is increasing year by year,the sulfur content of the crude oil is also increasing, the sulfur content in tail gas at the top of a constant-pressure reduction tower of an oil refinery is also increasing, and general H is2The S content is as high as 30-40%, so the existing top-reduced tail gas must be subjected to desulfurization treatment, and sulfur in the tail gas is recovered, so that the tail gas reaches the environmental-friendly emission standard.
At present, the domestic desulfurization method of the top-reducing tail gas is a regeneration recovery method, which generally adopts a tower-type absorption process, adopts a compressor to compress and pressurize the top-reducing gas, and the top-reducing tail gas and an amine liquid (mainly a methyldiethanolamine solution) are in countercurrent contact in a packed tower to achieve the aim of desulfurization. However, with the extension of the start-up period, the surface of the filler in the filler tower in the tower-type desulfurization device is easily blocked by the degradation products to form a channeling, which affects the mass transfer efficiency, and in severe cases, the whole circulation channel is covered by the degradation products, which causes the problem that the amine liquid cannot be settled and needs to be stopped for cleaning.
Disclosure of Invention
The invention aims to solve the technical problem of providing a complete equipment for reducing the top pressure and desulfurizing, which has simple structure, reliable operation, high efficiency and low cost.
The invention also provides a desulfurization process which does not need filler, fully mixes gas and liquid and has good desulfurization effect.
The technical scheme adopted by the invention for solving the problems is as follows: the top-reducing pressurized desulfurization complete equipment comprises a pressurized injection device, a solution tank, a circulating pump device, a rich liquid pump device and a cooler device, wherein the pressurized injection device is connected with the solution tank, the solution tank is connected with the circulating pump device and the rich liquid pump device, and the circulating pump device is sequentially connected with the cooler device and the pressurized injection device to form a loop.
The device is also provided with a liquid outlet flow control device, a working liquid flow control device and a liquid inlet flow control device, wherein the liquid outlet flow control device is connected with the rich liquid pump device, the working liquid flow control device is positioned between the cooler device and the pressurizing and jetting device, and the liquid inlet flow control device is connected with the solution tank.
The device is also provided with a methyldiethanolamine rich solution regeneration device and a methyldiethanolamine solution inlet device, and the liquid outlet flow control device is connected with the solution tank through the methyldiethanolamine rich solution regeneration device and the methyldiethanolamine solution inlet device.
The desulfurization process using the complete equipment for top-reducing and pressurizing desulfurization uses methyldiethanolamine solution [ (CH3) N (CH2CH2OH)2]As a desulfurizing agent, the method comprises the following specific steps,
(1) high-pressure methyldiethanolamine solution sucks untreated high-sulfur-content reduced-top tail gas through a pressurized spraying device, and the reduced-top tail gas and the methyldiethanolamine solution are fully mixed and pressurized in the pressurized spraying device, so that the high-sulfur-content reduced-top tail gas and the methyldiethanolamine solution are fully mixed and pressurized in the pressurized sprayingdevice to ensure that the high-sulfur-H in the reduced-ceiling tail gas2S and a methyldiethanolamine solution generate an absorption reaction;
(2) discharging a gas-liquid mixture generated after the reaction of the top-reducing tail gas and the methyldiethanolamine solution into a solution tank to ensure that H in the top-reducing tail gas2S, after carrying out absorption reaction with the methyldiethanolamine solution in the solution tank again, discharging gas reaching the purification standard concentration;
(3) solution tank absorbs H2The methyldiethanolamine solution of S becomes methyldiethanolamine rich solution [ (CH3) N.H2S. (CH2CH2OH)2]Discharging the methyldiethanolamine rich solution to a methyldiethanolamine rich solution regeneration device through a rich solution pump device for regeneration;
(4) and (2) taking the regenerated methyldiethanolamine solution as a desulfurizing agent again, feeding the regenerated methyldiethanolamine solution into the solution tank through a methyldiethanolamine solution feeding device, simultaneously supplementing a fresh methyldiethanolamine solution to replace a methyldiethanolamine solution rich solution in the solution tank, reducing the concentration of the methyldiethanolamine solution rich solution in the solution tank, pressurizing the mixed methyldiethanolamine solution through a circulating pump device, cooling the mixed methyldiethanolamine solution through a cooler device, and finally feeding the mixed methyldiethanolamine solution into a pressurizing and spraying device to provide power for sucking untreated high-sulfur-content topping off gas in the step (1.
When the methyldiethanolamine rich solution in the step (3) is discharged from the rich solution pump device to the methyldiethanolamine rich solution regeneration device, the flow is controlled bythe liquid outlet flow control device; controlling the flow of the methyldiethanolamine solution in the step (4) through a liquid inlet flow control device when the methyldiethanolamine solution enters the solution tank through a methyldiethanolamine solution inlet device; and (4) controlling the flow of the methyldiethanolamine solution cooled by the cooler device in the step (4) through a working fluid flow control device when the methyldiethanolamine solution enters the pressurizing and spraying device.
The mass percentage concentration of the methyldiethanolamine solution as the desulfurizing agent in the step (1) of the invention is 30%.
The volume percentage concentration of the untreated high-sulfur-content top-reduced tail gas in the step (1) is 30-40%.
The mass percentage concentration of the methyldiethanolamine rich solution [ (CH3) N.H2S. (CH2CH2OH)2]generated in the step (3) is 15-20%.
The concentration of H2S in the gas reaching the standard concentration for purification in step (2) of the invention is less than or equal to 2000 ppm.
The reduced-ceiling tail gas in the step (1) of the invention is pressurized to 0.2MPa in a pressurizing injection device.
Compared with the prior art, the top-reducing pressurizing desulfurization complete equipment has the following beneficial effects:
1. the whole set of equipment consists of a pressurizing injection device, a solution tank, a circulating pump device, a pregnant solution pump device, a cooler device and the like, and has simple structure and small equipment investment; 2. the pressurizing and jetting device can fully mix and pressurize the desulfurizer and the reduced-top tail gas, so that the desulfurizer fully absorbs H2S gas has good desulfurization effect, high pressurization and air extraction efficiency and low operation cost; 3. the equipment is not limited by gas temperature and working medium, has strong adaptability, does not need to be stopped and cleaned, and has low operation and maintenance cost.
Compared with the prior art, the desulfurization process using the complete equipment for reducing the top and pressurizing desulfurization has the following beneficial effects: 1. 30% methyldiethanolamine is used as desulfurizing agent for H2The S has high adsorption efficiency, can generate chemical adsorption reaction with acid gas at normal temperature (40-80 ℃) under high acid gas partial pressure, and then generates chemical adsorption reaction with the acid gasSteam is heated to 120 ℃ under low acid gas partial pressure for stripping regeneration, and especially, the methyldiethanolamine can quickly absorb H under the operating condition of short contact time2S is regenerated and recycled, the price of the S is 1/2-2/3 of wet desulphurization, no vaporization loss is caused during stripping regeneration, the S has high resistance to activity degradation caused by heat and chemical reaction, and the methyldiethanolamine also has low corrosivity and H2S has the advantages of low reaction heat, less steam consumption and low solubility to hydrocarbon, so that the methyldiethanolamine absorbs H2The optimal solvent for S; 2. the adopted top-reducing tail gas pressurizing and jetting desulfurization technology makes up the defects of a tower-type desulfurization process, and utilizes the full mixing and pressurizing of the desulfurizing agent and the top-reducing tail gas to ensure that the desulfurizing agent can more fully absorb H2S gas does not need to be filled, the absorption effect is good, and the blank of pressurizing desulfurization of the reduced-ceiling tail gas by adopting a pressurizing jet desulfurizer in China is filled.
Drawings
FIG. 1 is a schematic view showing the construction of a top-reduced, pressurized desulfurization plant according to the present invention.
FIG. 2 is a flow diagram of a desulfurization process using a reduced-ceiling, pressurized desulfurization plant in accordance with the present invention.
Detailed Description
Example of a reduced-ceiling pressurized desulfurization plant:
referring to fig. 1, the top-reducing pressurized desulfurization complete equipment in the invention is composed of a pressurized spraying device I, a solution tank II, a circulating pump device III, a pregnant solution pump device VI, a cooler device IV, a liquid outlet flow control device VII, a working solution flow control device V, a liquid inlet flow control device VIII, a methyldiethanolamine pregnant solution regeneration device IX and a methyldiethanolamine solution inlet device X.
The pressurized injection device I comprises a first manual valve 1-1, a first filter 2, a first pressure transmitter 3-1, a pressurized injector 4 and a second manual valve 5, wherein the first manual valve 1-1, the first filter 2, the first pressure transmitter 3-1 and the pressurized injector 4 are sequentially connected through a pipeline, one end of the second manual valve 5 is connected with the pipeline between the pressurized injector 4, and the other end of the second manual valve is a reduced-top tail gas inlet.
The solution tank II comprises a methyldiethanolamine tank 6, a nineteenth manual valve 7-4, a twentieth manual valve 8 and a second pressure transmitter 3-2, wherein the nineteenth manual valve 7-4, the twentieth manual valve 8 and the second pressure transmitter 3-2 are connected with the methyldiethanolamine tank 6.
The liquid inlet flow control device VIII comprises a seventeenth manual valve 7-1, a first regulating valve 24, an eighteenth manual valve 7-2, a first flow meter 25 and a sixteenth manual valve 7-3, wherein the seventeenth manual valve 7-1, the first regulating valve 24, the eighteenth manual valve 7-2 and the first flow meter 25 are sequentially connected with a nineteenth manual valve 7-4 through pipelines, and two ends of the sixteenth manual valve 7-3 are connected with one end of the nineteenth manual valve 7-4 and one end of the first flow meter 25. The first flow meter 25 is in turn connected to a methyldiethanolamine solution feed unit X.
The liquid enrichment pump device VI comprises an eleventh manual valve 10, a third filter 18, a methyldiethanolamine liquid enrichment pump 21, a third pressure transmitter 3-4, a first one-way check valve 20, a twelfth manual valve 19-4, the eleventh manual valve 10, the third filter 18, the methyldiethanolamine liquid enrichment pump 21, the third pressure transmitter 3-4, the first one-way check valve 20 and the twelfth manual valve 19-4 which are sequentially connected with the methyldiethanolamine tank 6 through pipelines.
The effluent liquid flow control device VII comprises a third flow meter 22, a fifteenth manual valve 19-2, a third regulating valve 23, a fourteenth manual valve 19-1 and a thirteenth manual valve 19-3, wherein the third flow meter 22, the fifteenth manual valve 19-2, the third regulating valve 23, the fourteenth manual valve 19-1 and the thirteenth manual valve 19-3 are sequentially connected with a twelfth manual valve 19-4 through pipelines, and two ends of the thirteenth manual valve 19-3 are connected with one end of the fifteenth manual valve 19-2 and one end of the fourteenth manual valve 19-1. The fourteenth manual valve 19-1 is connected with a methyldiethanolamine pregnant solution regeneration device IX.
The circulating pump device III comprises a tenth manual valve 9, a second filter 11, a methyldiethanolamine circulating pump 13, a second one-way check valve 12 and ninth manual valves 1-5, wherein the tenth manual valve 9, the second filter 11, the methyldiethanolamine circulating pump 13, the second one-way check valve 12 and the ninth manual valves 1-5 are sequentially connected with the methyldiethanolamine tank 6 through pipelines.
The cooler device IV comprises eighth manual valves 1-7, a methyldiethanolamine cooler 14, sixth manual valves 1-6, fourth pressure transmitters 3-3 and seventh manual valves 15-1, one end of the sixth manual valve 1-6 is connected with the ninth manual valve 1-5, the other end of the sixth manual valve is connected with the methyldiethanolamine cooler 14, and the fourth pressure transmitters 3-3, the seventh manual valve 15-1 and the eighth manual valves 1-7 are connected with the methyldiethanolamine cooler 14 through pipelines.
The working fluid flow control device V comprises a second flow meter 16, a fifth manual valve 1-3, a second regulating valve 17, a fourth manual valve 1-2 and a third manual valve 1-4, an eighth manual valve 1-7 is connected with the second flow meter 16, the fifth manual valve 1-3, the second regulating valve 17, the fourth manual valve 1-2 and the first manual valve 1-1 sequentially through pipelines, and two ends of the third manual valve 1-4 are connected with one end of the fifth manual valve 1-3 and one end of the fourth manual valve 1-2.
The pressurizing ejector device I is key equipment of the invention and has the function of reacting a desulfurizing agent with the top-reduced tail gasThe location is provided, and the pressurization, mixing and reaction of the top-reduced tail gas and the desulfurizer are all completed in the pressurization ejector 4. The high-pressure methyldiethanolamine solution enters a receiving chamber through a nozzle in a high-speed flow, the reduced-head tail gas is sucked and mixed with the reduced-head tail gas and subjected to energy exchange, the methyldiethanolamine solution is mixed with gas to form emulsified liquid, the emulsion and the jet flow are converged, further mixed along an ejector mixing chamber and then enter a diffuser, and the gas-liquid mixture in a flowing state is boosted through the diffuser and then discharged out of a booster ejector 4. In the whole process, when the top-reduced tail gas is contacted with methyldiethanolamine, H in the tail gas2S reacts rapidly with methyldiethanolamine, H2S is absorbed by methyldiethanolamine, and H in the reduced-top tail gas is fully mixed with the methyldiethanolamine and pressurized2S is well absorbed by methyldiethanolamine.
The solution tank II is used for receiving the gas-liquid mixture discharged from the booster ejector 4 and mixing the gas-liquid mixture with the methyl diethyl etherThe methyldiethanolamine solution in the alcohol amine tank 6 is further subjected to contact reaction to remove H in the gas2And S, separating the gas which cannot be absorbed and reacted with the methyldiethanolamine from the solution in the tank and then discharging the gas. Absorption of H2And (3) converting the methyldiethanolamine of the S gas into a rich solution, discharging a part of the rich solution through a rich solution pump device VI, receiving a fresh methyldiethanolamine solution provided by the device, mixing the fresh methyldiethanolamine solution with the methyldiethanolamine solution in the tank, and reducing the concentration of the desulfurizer rich solution in the tank.
The rich liquid pump device VI has the function of discharging a part of rich liquid from the tank to the methyldiethanolamine rich liquid regeneration device IX, and the flow rate of the rich liquid is controlled by the liquid outlet flow control device VII. The rich solution heats H by steam2S is separated from the methyldiethanolamine solution, and H is separated2S is recovered, and the separated solution is reused as fresh liquid.
The liquid inlet flow control device VIII is used for controlling the flow of the added fresh desulfurizer, the liquid outlet flow control device VII is used for controlling the given flow of the liquid enrichment pump device VI, and the two sets of flow control devices jointly control the concentration of the rich liquid of the desulfurizer.
The circulating pump device III is used for pressurizing the desulfurizer to provide power for the pressurizing ejector 4, and the pressure of the pressurized desulfurizer is adjusted according to different processes. The cooler device IV is used for cooling the temperature of the desulfurizer and mixing the desulfurizer with H2And the heat of the S reaction is discharged from the device, so that the temperature of the desulfurizer is ensured to be less than 40 ℃.
The working fluid flow control device V is used for controlling the flow of the working medium of the booster ejector 4 and controlling the ratio of the desulfurizer to the reduced-ceiling tail gas under the most reasonable condition.
Absorption of H by methyldiethanolamine2The chemical mechanism of S:
in the acid gas, H2S is a proton donating proton donor Bronsted acid which forms hydrogen sulfide ions (hydrosulfition) via proton transfer reaction when reacted with methyldiethanolamine,this reaction is a fairly rapid, almost instantaneous reaction, which is a condensation reaction, and has the following formula:
from the above reaction formula, it is known that methyldiethanolamine absorbs H2S, which absorbs 1.0mola of H per mola of methyldiethanolamine2S gas
Because the sulfur content of the reduced-ceiling tail gas is very high and is generally 30-40%, in order to ensure that the gas after desulfurization and purification contains less than 2000ppm, the concentration of the pregnant solution in the absorbed methyldiethanolamine solution must be controlled within 15-17%, so that 1.0kg of H is absorbed2The S gas generates 69-78 kg of rich liquid.
Examples of desulfurization processes using a reduced-ceiling pressurized desulfurization plant:
referring to fig. 2, the process comprises the specific steps of,
(1) absorbing untreated high-sulfur-content top-reducing tail gas by using 30 mass percent methyldiethanolamine solution through a pressurizing and spraying device I, wherein the flow rate of the top-reducing tail gas is 800kg/H, the pressure is 800mmHg, and the top-reducing tail gas contains H2The S concentration is 40 percent, the temperature is 40 ℃, the top-reducing tail gas and the methyldiethanolamine solution are fully mixed in a pressurizing and spraying device I and pressurized to the pressure of 0.2MPa, and H in the top-reducing tail gas2S and a methyldiethanolamine solution generate an absorption reaction;
(2) discharging a gas-liquid mixture generated after the reaction of the reduced-ceiling tail gas and the methyldiethanolamine solution into a solution tank II (the volume of the solution tank is 45 m)3) H in medium, reduced top tail gas2S again generates absorption reaction with the methyldiethanolamine solution in the solution tank, gas reaching the purification standard concentration is discharged, the concentration of H2S in the purified gas is less than or equal to 2000ppm, and the purified gas is discharged into the incinerator;
(3) solution tank II absorbs H2The methyldiethanolamine solution of S is 18 percent of methyldiethanolamine rich solution [ (CH3) N.H2S. (CH2CH2OH)2]The concentration of the methyldiethanolamine rich solution is 30m3The flow of the flow/h is discharged into a methyldiethanolamine rich solution regeneration device IX through a rich solution pump device VI for regeneration, and the flow of the flow is controlled through a liquid outlet flow control device VII;
(4) the regenerated methyldiethanolamine solution is used as a desulfurizer again, enters the solution tank II through the methyldiethanolamine solution feeding device X and is 30m in length3Supplementing fresh methyldiethanolamine solution at flow rate of/h to replace the methyldiethanolamine solution rich solution in the solution tank II and reduce the concentration of the methyldiethanolamine solution in the solution tank II, pressurizing the mixed methyldiethanolamine solution to 1.9Mpa by a circulating pump device III, and then passing through a cooler device IV (the heat exchange area of a cooler is 160 m)2) Cooling, and pressing at 85m3And h, enabling the flow rate to enter a pressurizing and spraying device I to provide power for sucking untreated high-sulfur-content top-reduced tail gas in the step (1), wherein the flow rate is controlled by a liquid inlet flow control device VIII.
Claims (10)
1. A top-reducing pressurizing desulfurization complete equipment is characterized in that: the device comprises a pressurizing and spraying device, a solution tank, a circulating pump device, a rich liquid pump device and a cooler device, wherein the pressurizing and spraying device is connected with the solution tank, the solution tank is connected with the circulating pump device and the rich liquid pump device, and the circulating pump device is sequentially connected with the cooler device and the pressurizing and spraying device to form a loop.
2. The reduced-ceiling pressurized desulfurization plant of claim 1, characterized in that: the liquid outlet flow control device is connected with the rich liquid pump device, the working liquid flow control device is positioned between the cooler device and the pressurizing and jetting device, and the liquid inlet flow control device is connected with the solution tank.
3. The reduced-ceiling pressurized desulfurization plant according to claim 1 or 2, characterized in that: the system is also provided with a methyldiethanolamine rich solution regeneration device and a methyldiethanolamine solution inlet device, and the effluent liquid flow control device is connected with the solution tank through the methyldiethanolamine rich solution regeneration device and the methyldiethanolamine solution inlet device.
4. A desulfurization process using the reduced-ceiling pressurized desulfurization plant of claim 1, using methyldiethanolamine solution [ (CH3) N (CH2CH2OH)2]The desulfurizer is characterized in that: the method comprises the specific steps of carrying out,
(1) high-pressure methyldiethanolamine solution sucks untreated high-sulfur-content reduced-ceiling tail gas through a pressurized spraying device, the reduced-ceiling tail gas and the methyldiethanolamine solution are fully mixed in the pressurized spraying device and pressurized, and H in the reduced-ceiling tail gas is enabled to be2S and a methyldiethanolamine solution generate an absorption reaction;
(2) discharging a gas-liquid mixture generated after the reaction of the top-reducing tail gas and the methyldiethanolamine solution into a solution tank to ensure that H in the top-reducing tail gas2S, after carrying out absorption reaction with the methyldiethanolamine solution in the solution tank again, discharging gas reaching the purification standard concentration;
(3) solution tank absorbs H2The methyldiethanolamine solution of S becomes methyldiethanolamine rich solution [ (CH3) N.H2S. (CH2CH2OH)2]Discharging the methyldiethanolamine rich solution to a methyldiethanolamine rich solution regeneration device through a rich solution pump device for regeneration;
(4) and (2) taking the regenerated methyldiethanolamine solution as a desulfurizing agent again, feeding the regenerated methyldiethanolamine solution into the solution tank through a methyldiethanolamine solution feeding device, simultaneously supplementing a fresh methyldiethanolamine solution to replace a methyldiethanolamine solution rich solution in the solution tank, reducing the concentration of the methyldiethanolamine solution rich solution in the solution tank, pressurizing the mixed methyldiethanolamine solution through a circulating pump device, cooling the mixed methyldiethanolamine solution through a cooler device, and finally feeding the mixed methyldiethanolamine solution into a pressurizing and spraying device to provide power for sucking untreated high-sulfur-content topping off gas in the step (1.
5. The desulfurization process using a reduced-pressure desulfurization plant according to claim 4, characterized in that: when the methyldiethanolamine rich solution in the step (3) is discharged from the rich solution pump device to the methyldiethanolamine rich solution regeneration device, the flow rate is controlled by a liquid outlet flow rate control device; controlling the flow of the methyldiethanolamine solution in the step (4) through a liquid inlet flow control device when the methyldiethanolamine solution enters the solution tank through a methyldiethanolamine solution inlet device; and (4) controlling the flow of the methyldiethanolamine solution cooled by the cooler device in the step (4) through a working fluid flow control device when the methyldiethanolamine solution enters the pressurizing and spraying device.
6. The desulfurization process using a reduced-ceiling pressurized desulfurization plant according to claim 4, characterized in that: the mass percentage concentration of the methyldiethanolamine solution used as the desulfurizing agent in the step (1) is 30%.
7. The desulfurization process using a reduced-ceiling pressurized desulfurization plant according to claim 4, characterized in that: the volume percentage concentration of the untreated high-sulfur-content top-reduced tail gas in the step (1) is 30-40%.
8. The desulfurization process using a reduced-ceiling pressurized desulfurization plant according to claim 4, characterized in that: the mass percentage concentration of the methyldiethanolamine rich solution [ (CH3) N.H2S. (CH2CH2OH)2]generated in the step (3) is 15-20%.
9. The desulfurization process using a reduced-ceiling pressurized desulfurization plant according to claim 4, characterized in that: the concentration of H2S in the gas reaching the standard purification concentration in the step (2) is less than or equal to 2000 ppm.
10. The desulfurization process using a reduced-ceiling pressurized desulfurization plant according to claim 4, characterized in that: and (3) pressurizing the reduced-top tail gas in the step (1) to 0.2MPa in a pressurizing injection device.
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| CN102357484A (en) * | 2011-10-07 | 2012-02-22 | 刘军 | Mechanical filler cleaning method and mechanical filler cleaning device |
| CN103111175A (en) * | 2013-02-20 | 2013-05-22 | 北京三聚环保新材料股份有限公司 | Desulfurization device for purifying gas |
| CN104307341A (en) * | 2014-11-06 | 2015-01-28 | 上海齐耀螺杆机械有限公司 | Flare gas compression and desulphurization technology |
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