CN101092576A - Method for removing acid gases in cracked gas - Google Patents
Method for removing acid gases in cracked gas Download PDFInfo
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- CN101092576A CN101092576A CN 200610086618 CN200610086618A CN101092576A CN 101092576 A CN101092576 A CN 101092576A CN 200610086618 CN200610086618 CN 200610086618 CN 200610086618 A CN200610086618 A CN 200610086618A CN 101092576 A CN101092576 A CN 101092576A
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Abstract
This invention provides a method for removing acidic gas from cracked gas. The method comprises: introducing cracked gas containing acidic gas through a gas inlet into a super-gravitational revolving bed device, adequately contacting with alkaline absorbent or water in the rotor filler layer, removing acidic gas, and exhausting through a gas outlet to obtain cracked gas with acidic gas content below 1 ppm. The method has such advantages as low apparatus investment, low energy consumption, low operation cost, and low apparatus space occupation.
Description
Technical field
The present invention relates to a kind of method that removes the sour gas in the splitting gas, specifically, relate to a kind of method of using high-gravity rotating bed technology to remove sour gas in the splitting gas.
Background technology
Industrial, (be referred to as: sour gas), sour gas is bigger to the harm that later separation causes to contain hydrogen sulfide, carbonic acid gas and organosulfur in the splitting gas of preparing ethylene by steam cracking usually.At first, severe corrosion equipment when sulphur content is high shortens the work-ing life of equipment, and simultaneously, sulphur can also make the molecular sieve lost of life of dry splitting gas, and the used palladium catalyst of acetylene removal is poisoned.Secondly, carbonic acid gas is formed dry ice occluding device and pipeline easily in follow-up low ternperature separation process operating process, destroys ordinary production.The more important thing is that acid gas impurities also has harm for ethylene product, for example, in the ethylene polymerisation process, carbonic acid gas and sulfide can make the metal carbon bond of polymerizing catalyst decompose, and destroy its catalytic activity; In the high pressure polymerization of ethylene process, carbonic acid gas accumulates in cyclic ethylene, has reduced ethylene partial pressure, thereby influences polymerization velocity and poly molecular weight.Therefore the sour gas in the splitting gas must be removed.
General requirement with acid gas removal in the splitting gas to less than 1ppm.Usually the method that adopts has hot salt of wormwood washing method, sodium hydroxide washing method (hereinafter to be referred as alkali cleaning) and ethanolamines solution absorption method.Sulphur mass content≤0.1% o'clock in the industrial cracking stock, the content of acid gas in the splitting gas is lower, adopts alkali wash most economical; When the sulphur mass content was 0.1%-0.5% in the cracking stock, the content of acid gas in the splitting gas was higher, and is single very big, uneconomical with the alkali wash alkali consumption.Single again can not organic sulfide removal with the ethanolamines solution absorption, the method that needs to adopt the ethanolamines solution absorption method to combine with alkali wash is come combine operations.Promptly remove a large amount of sour gas, remove remaining sour gas with alkali wash again with the ethanolamines solution absorption method; When sulphur mass content in the cracking stock＞0.5%, to carry out desulfurization to raw material before the cracking.
The removal methods of sour gas in the splitting gas in the prior art, technological process is that splitting gas is an absorption agent with ethanolamines solution and/or alkali lye, in the absorption tower, absorb sour gas through circulation, behind the alkali that the washing flush away is carried secretly, leave the system of removing (" ethylene process and technology ", Wang Songhan, what thin lotus root chief editor, Sinopec press again, 2000,6, pp367-383 introduces the present invention as a reference).Wherein alkali cleaning flow process mainly is divided into two classes, that is, and and two sections alkali cleanings of one section washing and three sections alkali cleanings of one section washing.KTI/TPL company adopts two sections alkali cleanings, two sections alkali cleanings of the also many employings of Linde Co, and three sections alkali cleaning flow processs that one weber of special company of stone, Lu Musi company etc. adopt, but the consumption of alkali lye is all very big.
What above-mentioned sour gas removal methods was adopted all is tower equipment, and the volume of equipment is big, and pressure drop is big and high, the energy consumption height, and investment is many; Because the gas-to-liquid contact effect on absorption tower is relatively poor, and mass-transfer efficiency is lower,, have to strengthen the specific absorption of circulating fluid volume, so process cost improves significantly in addition with raising alkali washing process sour gas so assimilated efficiency is lower.
Summary of the invention
In order to overcome the defective that facility investment is big, assimilated efficiency is low, process cost is high of using the absorption tower technology to remove the method existence of the sour gas in the splitting gas in the prior art, the invention provides a kind of method of using high-gravity rotating bed technology to remove the sour gas in the splitting gas.
The method that removes sour gas in the splitting gas of the present invention, be with the splitting gas of acid gas-containing after hypergravity swinging bed device is introduced in the gas phase import, in its rotor packing layer, fully contact with alkaline absorbent or water, after strong mass transfer removes sour gas, discharge from gaseous phase outlet, obtain the splitting gas of content of acid gas less than 1ppm.Afterwards, the splitting gas of discharging can be introduced subsequent drying workshop section and carry out drying, and then enter next procedure.
With splitting gas by the gas phase import of hypergravity swinging bed device tangentially in the introducing device, outer rim inner edge to the rotor packing layer under differential pressure action through the rotating rotor packing layer flows, alkaline absorbent or water are in the liquid phase import access to plant of hypergravity swinging bed device, liquid distributor through the center evenly is sprayed on the inner edge of rotor packing layer, under powerful centrifugal action, outwards flow by inner edge, gas-liquid two-phase is gone against the stream, under the situation that strong turbulence fully contacts on the rotor packing layer, carry out physical absorption and chemical absorption, then gas phase is drawn by the gaseous phase outlet of device and is entered next procedure, and absorption agent is drawn by its liquid phase outlet.
Concrete, the method that removes sour gas in the splitting gas of the present invention may further comprise the steps:
1) alkali cleaning step:
Splitting gas, the alkaline absorbent of acid gas-containing are introduced at least one section alkali cleaning hypergravity swinging bed device through gas phase import, liquid phase import respectively;
In the rotor packing layer of described device, described splitting gas is drawn by gaseous phase outlet, to washing hypergravity swinging bed device or next section alkali cleaning hypergravity swinging bed device with after alkaline absorbent contacts;
After described alkaline absorbent absorbs sour gas, drawn by the liquid phase outlet, wherein a part is drawn as waste liquid, to the liquid waste disposal district; Part absorption liquid is introduced and to be arranged in the middle circulation tank in liquid phase exit, with fresh alkaline absorbent or from after the partially absorbing liquid and mix of the middle circulation tank of next section alkali cleaning hypergravity swinging bed device, recycles;
2) water-washing step:
Splitting gas, water that step 1) obtains are introduced in the washing hypergravity swinging bed device through gas phase import, liquid phase import respectively;
In the rotor packing layer of described device, described splitting gas is drawn by gaseous phase outlet with after water contacts;
Behind the alkali lye of carrying secretly in the described water washing splitting gas, draw, to the middle circulation tank that is arranged at this device liquid phase exit, recycle by the liquid phase outlet.
The present invention does not have particular requirement for alkaline absorbent, and the alkaline absorbent that is used for removing the splitting gas sour gas in the prior art all can use.In a preferred embodiment of the invention, described fresh alkaline absorbent is selected from a kind of in sodium hydroxide solution, potassium hydroxide solution and the hot potassium carbonate solution or their mixture.More preferably, use sodium hydroxide solution.
In the method for the invention, described alkali cleaning step 1) can be one section alkali cleaning, two sections alkali cleanings or three sections alkali cleanings, and promptly splitting gas can be introduced in one, two or three the alkali cleaning hypergravity swinging bed devices, removes sour gas wherein.
In a preferred embodiment of the invention, described alkali cleaning step is two sections alkali cleanings, comprises the following steps:
A) splitting gas of described acid gas-containing, one section alkaline absorbent are introduced respectively in one section alkali cleaning hypergravity swinging bed device, described splitting gas is with after one section alkaline absorbent contacts in its rotor packing layer, draw by gaseous phase outlet, to two sections alkali cleaning hypergravity swinging bed devices; After described one section alkaline absorbent absorbs sour gas, drawn by the liquid phase outlet, wherein a part is drawn as waste liquid, to the liquid waste disposal district; In the circulation tank, the two sections absorption liquids of part with from two sections middle circulation tanks recycled as one section alkaline absorbent in the middle of part absorption liquid was introduced one section that is arranged at the liquid phase exit;
B) splitting gas that step a) is obtained, two sections alkaline absorbents are introduced respectively in two sections alkali cleaning hypergravity swinging bed devices, described splitting gas is with after two sections alkaline absorbents contact in its rotor packing layer, draw by gaseous phase outlet, wash to washing in the hypergravity swinging bed device; The part of described two sections absorption liquids is introduced one section as one section additional liquid; In the middle of introducing two sections that are arranged at the liquid phase exit, part absorption liquid in the circulation tank,, recycles as two sections alkaline absorbents with fresh alkaline absorbent.
In concrete enforcement, preferably the splitting gas with described acid gas-containing is preheating to 40 ℃-45 ℃, tangentially introduce in one section alkaline cleaner through the import of one section alkali cleaning hypergravity swinging bed device gas phase again, go against the stream with the alkaline absorbent that comes by the liquid phase import in the rotor packing layer in described device, contact fully and mass transfer, after removing the sour gas in the splitting gas, after the rotation mist eliminator that is arranged on one section alkali cleaning hypergravity swinging bed device rotor center place is caught foam, discharge one section alkali cleaning hypergravity swinging bed device, enter two sections alkali cleaning hypergravity swinging bed devices through the gas phase import; In two sections alkali cleaning hypergravity swinging bed devices, similarly contact and mass transfer, further remove the sour gas in the splitting gas after, enter the washing hypergravity swinging bed device; Go against the stream with the water that comes by the liquid phase import in the rotor packing layer in the washing hypergravity swinging bed device, contact fully, the alkali mist that the flush away splitting gas is carried secretly, after the rotation mist eliminator of washing high-gravity rotating bed rotor center place is caught foam, through washing the catching after the foam jar catches foam of high-gravity rotating bed gaseous phase outlet, enter subsequent handlings such as drying process drying again.
In the specific embodiments of two sections alkali cleaning flow processs of the present invention, the mass percent concentration of the fresh alkaline absorbent solute that is contained in described one section alkaline absorbent is 0%-2%, and the mass percent concentration of the fresh alkaline absorbent solute that is contained in two sections alkaline absorbents is 8%-15%.More preferably, described fresh alkaline absorbent is that mass percent concentration is the sodium hydroxide solution of 20%-30%, the mass percent concentration of sodium hydroxide is 0%-2% in one section alkaline absorbent, and the mass percent concentration of sodium hydroxide is 8%-15% in two sections alkaline absorbents.
In another preferred embodiment of the present invention, described alkali cleaning step is three sections alkali cleanings, comprises the following steps:
A) splitting gas of described acid gas-containing, one section alkaline absorbent are introduced respectively in one section alkali cleaning hypergravity swinging bed device, described splitting gas is with after one section alkaline absorbent contacts in its rotor packing layer, draw by gaseous phase outlet, to two sections alkali cleaning hypergravity swinging bed devices; After described one section alkaline absorbent absorbs sour gas, drawn by the liquid phase outlet, wherein a part is drawn as waste liquid, to the liquid waste disposal district; In the circulation tank, the two sections absorption liquids of part with from two sections middle circulation tanks recycled as one section alkaline absorbent in the middle of part absorption liquid was introduced one section that is arranged at the liquid phase exit;
B) splitting gas that step a) is obtained, two sections alkaline absorbents are introduced respectively in two sections alkali cleaning hypergravity swinging bed devices, described splitting gas is with after two sections alkaline absorbents contact in its rotor packing layer, draw by gaseous phase outlet, to three sections hypergravity swinging bed devices; The part of described two sections absorption liquids is introduced one section as one section additional liquid; In the circulation tank, the three sections absorption liquids of part with from three sections middle circulation tanks recycled as two sections alkaline absorbents in the middle of part absorption liquid was introduced two sections that are arranged at the liquid phase exit;
C) splitting gas that step b) is obtained, three sections alkaline absorbents are introduced respectively in three sections alkali cleaning hypergravity swinging bed devices, described splitting gas is with after three sections alkaline absorbents contact in its rotor packing layer, draw by gaseous phase outlet, wash to washing in the hypergravity swinging bed device; The part of described three sections absorption liquids is introduced two sections as two sections additional liquid; In the middle of introducing three sections that are arranged at the liquid phase exit, part absorption liquid in the circulation tank,, recycles as three sections alkaline absorbents with fresh alkaline absorbent.
In the specific embodiments of three sections alkali cleaning flow processs of the present invention, the mass percent concentration of the fresh alkaline absorbent solute that is contained in described one section alkaline absorbent is 0%-2%, the mass percent concentration of the fresh alkaline absorbent solute that is contained in two sections alkaline absorbents is 6%-8%, and the mass percent concentration of the fresh alkaline absorbent solute that is contained in three sections alkaline absorbents is 12%-15%.More preferably, described fresh alkaline absorbent is that mass percent concentration is the sodium hydroxide solution of 20%-30%, the mass percent concentration of sodium hydroxide is 0%-2% in one section alkaline absorbent, the mass percent concentration of sodium hydroxide is 6%-8% in two sections alkaline absorbents, and the mass percent concentration of sodium hydroxide is 12%-15% in three sections alkaline absorbents.
In the method for the invention, the amount of absorption liquid of replenishing liquid as the preceding paragraph is as the amount of the fresh alkaline absorbent of two sections additional liquid or introducing, is that the amount of the waste liquid that enters the liquid waste disposal operation of being drawn by the liquid phase outlet of one section alkali cleaning hypergravity swinging bed device is determined.Concrete, for two sections alkali cleanings, one section insufficient part of alkaline absorbent is replenished by two sections absorption liquids, two sections insufficient parts of alkaline absorbent are replenished by fresh alkaline absorbent, by carrying out material balance, control the concentration that contains fresh alkaline absorbent solute in every section the alkaline absorbent, be easy to determine to replenish the amount of liquid.
The splitting gas of the acid gas-containing that method of the present invention is related from five sections compressors in the cracking technology before or each section compressor outlet.Specifically, the splitting gas of described acid gas-containing from compressor before or compressor one section outlet or second stage exit or three sections outlets or four sections outlets or five sections outlets, be preferably three sections outlets of compressor or four sections outlets.
In aforesaid method of the present invention, the rotating speed of described hypergravity swinging bed device is 50-1500rpm, and the filler that uses in the described rotor packing layer is corrugated metal wire packing or waved plate butterfly filler.There is no particular limitation to the specific surface area of used filler and porosity.
In aforesaid method of the present invention, the splitting gas of preferred described acid gas-containing is that the cracking stock cracking by sulphur mass content≤0.1% obtains.
In the method for the invention, circulation tank in the middle of the liquid phase outlet of described alkali cleaning hypergravity swinging bed device and washing hypergravity swinging bed device is provided with, its effect is: 1) gas delivery of carrying secretly in separating liquid space is provided; 2) prevent that the liquid level in the hypergravity equipment is too high, flood rotor, thereby cause the excessive motor that burns of motor load, and liquid floods rotor and causes mass transfer effect to descend; 3) provide a fluid-tight, prevent that gas from liquid outlet from overflowing.
, can adjust when implementing above-mentioned method of the present invention concrete according to the difference of charging splitting gas content of acid gas.For guaranteeing that sour gas fully removes, at described splitting gas is to be under the cracking stock cracking of the 0.1%-0.5% situation about obtaining by the sulphur mass content, be that absorption agent removes a large amount of sour gas in the splitting gas in hypergravity swinging bed device at first with ethanolamines solution, and then carry out above-mentioned alkali cleaning step of the present invention and remove remaining sour gas in the splitting gas, adopt the alkali lye of carrying secretly in the water-washing step washing splitting gas then, to reduce the consumption of alkali in the follow-up alkaline cleaning procedure significantly.
Concrete, be to be under the cracking stock cracking of the 0.1%-0.5% situation about obtaining by the sulphur mass content at described splitting gas,
At first, splitting gas, the ethanolamines solution of acid gas-containing are introduced in the hypergravity swinging bed device, in its rotor packing layer, contact, make ethanolamines solution remove a large amount of sour gas in the described splitting gas, make the hydrogen sulfide content in the splitting gas reduce to 4.5-15ppm;
Then,, adopt aforesaid method of the present invention, in hypergravity swinging bed device, carry out alkali cleaning and washing, obtain the splitting gas of content of acid gas less than 1ppm with the above-mentioned splitting gas that removes a large amount of sour gas;
Preferably, described ethanolamines is selected from one or more in Monoethanolamine MEA BASF, diethanolamine, trolamine, methyldiethanolamine or the N methyldiethanol amine; More preferably diethanolamine, methyldiethanolamine or N methyldiethanol amine solution.Concentration to ethanolamines solution does not have particular requirement, and preferably its mass percent concentration is 25-30%.
Technical scheme related among the technical process that ethanolamines solution of the present invention removes a large amount of sour gas in the splitting gas and the Chinese patent application CN1608715A is similar.As shown in Figure 2, the splitting gas D of acid gas-containing is preheating to 40 ℃-45 ℃, tangentially enter the thanomin cleaning device through hypergravity swinging bed device 13 gas phase imports, go against the stream with the ethanolamines solution F that comes by its liquid phase import in the rotor packing layer in the thanomin cleaning device, contact fully with mass transfer with after removing the sour gas in the splitting gas, splitting gas G after removing a large amount of sour gas is after the rotation mist eliminator that is arranged on high-gravity rotating bed rotary filler layer center is once caught foam, again through being arranged on gaseous phase outlet catch the foam removal of foam jar secondary after, enter alkali cleaning flow process as shown in Figure 1.The rich amine liquid H that has absorbed sour gas enters liquid level controlling tank 17 through high-gravity rotating bed liquid phase outlet, under the pressure difference effect behind poor rich liquid heat exchanger 18, enter and be rich in hydrogen sulfide amine liquid Analytic Tower 14 and resolve, obtain taking off back sour gas I at the top of tower 14.
Be rich in hydrogen sulfide amine liquid Analytic Tower 14 and can adopt prior art packing tower or tray column (abbreviation Analytic Tower) commonly used.
In the method for the invention, used hypergravity swinging bed device adopts the described mesohigh of Chinese patent ZL01143459 not have the high-gravity rotating bed equipment of leakage.Hypergravity swinging bed device of the present invention adopts the corrosion resistant material preparation, as stainless steel, titanium material etc.
Method of the present invention has the following advantages:
1, under same production loading condiction, method of the present invention is compared with traditional absorption tower alkali washing process, and equipment takes up space and reduces greatly; And because the dispersion effect of liquid phase in high-gravity rotating bed is good, high-gravity rotating bed volume transmission quality coefficient is than the traditional high 1-3 of tower equipment order of magnitude, and the tower equipment of equipment pressure drop ratio tradition is little a lot of down for same load.
2, use method energy consumption of the present invention to reduce greatly, process cost is little;
3, the equipment of method use of the present invention is simple, invests low.
4, use method of the present invention, improved the utilization ratio of alkali, reduced the consumption of alkali.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for one section washing of two sections alkali cleanings of the present invention.
Fig. 2 is an ethanolamines solution washing schematic flow sheet.
The method of one section washing of two sections alkali cleanings of the present invention, as shown in Figure 1, the cracking gas D of described acid gas-containing is preheating to 40 ℃-45 ℃, tangentially introduce in one section alkaline cleaner through the 3 gas phase imports of one section alkali cleaning hypergravity swinging bed device again, go against the stream with the alkaline absorbent that is come by the liquid phase import in the rotor packing layer in described device, contact with mass transfer after, after the rotation mist eliminator that is arranged on one section alkali cleaning hypergravity swinging bed device, 3 rotor center places is caught foam, discharge one section alkali cleaning hypergravity swinging bed device, enter two sections alkali cleaning hypergravity swinging bed devices 2 through the gas phase import; In two sections alkali cleaning hypergravity swinging bed devices 2, similarly contact and mass transfer, further remove the sour gas in the cracking gas after, enter the washing hypergravity swinging bed device 1; Go against the stream with the water that is come by the liquid phase import in the rotor packing layer in washing hypergravity swinging bed device 1, contact fully, the alkali mist that the flush away cracking gas is carried secretly, after the rotation mist eliminator of washing high-gravity rotating bed rotor center place is caught foam, through washing the catching after the foam tank catches foam of high-gravity rotating bed gaseous phase outlet, the cracking gas B that obtains enters the subsequent handlings such as drying process drying again.
In Fig. 1,1 washing hypergravity swinging bed device, 2 two sections alkali cleaning hypergravity swinging bed devices, 3 one sections alkali cleaning hypergravity swinging bed devices, 4 fresh alkaline absorbent storage tanks, circulating tank in the middle of 5 washings, 6 two sections middle circulating tanks, circulating tank in the middle of 7 one sections, 8 fresh alkaline absorbent pumps, 9 water circulating pumps, 10 2 sections alkaline absorbent circulating pumps, 11 1 sections alkaline absorbent circulating pumps, 12 cracking gas preheaters; C fresh supplemented water, E introduces the waste liquid in liquid waste processing district
In Fig. 2: 13 monoethanolamines are washed hypergravity swinging bed device, 14 rich amine liquid Analytic Towers, 15 hot lean pumps, 16 poor amine liquid storage tanks, 17 liquid levels control tank, 18 poor rich liquid heat exchangers, 19 lean pumps, 20 lean solution coolers.
Embodiment
For a better understanding of the present invention, provide following examples, but the present invention is not limited to present embodiment.
Alkali cleaning workshop section below in conjunction with producing 800000 tons of ethylene processes per year compares using absorption tower and high-gravity rotating bed technological process of carrying out alkali cleaning respectively, with this effect of the present invention is described.
Produce 800000 tons of ethylene processes per year, the flow of splitting gas: 296.18 tons/hour, pressure 1698KPa, 46 ℃ of temperature are formed as table 1 in the splitting gas.The gas-liquid phase load such as the table 2 of each section.After treatment, make the total content of carbonic acid gas and hydrogen sulfide in the splitting gas less than 1ppm.
Table 1 splitting gas is formed (unit: mol%)
| H 2O | H 2 | CO | CO 2 | H 2S | CH 4 | C 2 | C 3 | C 4 | C 5More than |
| 0.39 | 16.04 | 0.09 | 0.01 | 0.02 | 26.46 | 39.48 | 10.83 | 4.55 | 1.02 |
Adopt one section washing process of two sections alkali cleanings of the present invention, schema as shown in Figure 1.Method of the present invention designs four hypergravity swinging bed devices altogether, and one standby, and technological process is as described in the specification sheets preamble.The comparing result of method of the present invention and prior art sees Table 2.
As can be seen from Table 2:
Use method of the present invention, device diameters has dwindled 38.7%, has highly reduced by 84.8%;
The total consumption of filler of the present invention is less than 3m
3, and the consumption of prior art filler m more than 270
3
The compressor power of saving is compared with the power of the consumption of hypergravity swinging bed device, and method of the present invention as can be known can be saved power KW more than 400;
In addition because the used equipment volume of the present invention is little, or, improved the corrosion resistance of equipment to use the corrosion resistant material manufacturing.The gross investment of equipment of the present invention lacks 37.2% than prior art.
The contrast of table 2 hypergravity alkali cleaning of the present invention and tower equipment alkali cleaning
| Technical indicator | Existing absorption tower | Method of the present invention (three open one is equipped with) | |
| Diameter m | 4.4 | 2.7 | |
| High m | 62.5 | 2.5+3.5×2 | |
| Shaft power KW | 0 | 8.8×3 | |
| Rotating speed r.p.m | 0 | 80-100 | |
| Cumulative volume m 3 | About 950 | About 55 | |
| Pressure drop Kpa | 78 | 3.9×3 | |
| The compressor power KW that saves | 0 | 448 | |
| Gas phase load kilogram/hour | 296180 | 296180 | |
| Liquid phase load ton/hour | Washing section | 9.37 | 9.33 |
| Three sections of alkali cleanings | 63.86 | 24.88 | |
| Two sections of alkali cleanings | 63.86 | / | |
| One section of alkali cleaning | 63.86 | 24.88 | |
| Plate number or amount of filler | Washing section | 3 bubble-caps | Ripple silk net filler 0.659m 3 |
| Three sections of alkali cleanings | IMTP50 filler 136.78m 3 | Ripple silk net filler 1.013m 3 | |
| Two sections of alkali cleanings | IMTP50 filler 136.78m 3 | / | |
| One section of alkali cleaning | 18 float valves | Ripple silk net filler 1.013m 3 | |
| Washing water pump shaft power KW | 0.613 | 0.613 | |
| Weak base recycle pump shaft power KW | 5.536 | 2.853 | |
| Middle alkali recycle pump shaft power KW | 5.56 | / | |
| Highly basic recycle pump shaft power KW | 5.569 | 2.86 | |
| Total shaft power KW of pump | 17.285 | 6.326 | |
| Operational circumstances | Easily stop up | Be difficult for stopping up | |
| Remove index (H 2S+CO 2)ppm | ＜1 | ＜1 | |
| Material | Housing carbon steel, internals and filler stainless steel | Housing carbon steel, internals stainless steel, rotor and filler titanium | |
| Corrosion-resistant | Generally | Excellent | |
| Invest/ten thousand yuan | 674 | 423 | |
Claims (12)
1, a kind of method that removes the sour gas in the splitting gas, it may further comprise the steps:
1) alkali cleaning step:
Splitting gas, the alkaline absorbent of acid gas-containing are introduced at least one section alkali cleaning hypergravity swinging bed device through gas phase import, liquid phase import respectively;
In the rotor packing layer of described device, described splitting gas is drawn by gaseous phase outlet, to washing hypergravity swinging bed device or next section alkali cleaning hypergravity swinging bed device with after alkaline absorbent contacts;
After described alkaline absorbent absorbs sour gas, drawn by the liquid phase outlet, wherein a part is drawn as waste liquid, to the liquid waste disposal district; Part absorption liquid is introduced and to be arranged in the middle circulation tank in liquid phase exit, with fresh alkaline absorbent or from after the partially absorbing liquid and mix of the middle circulation tank of next section alkali cleaning hypergravity swinging bed device, recycles;
2) water-washing step:
Splitting gas, water that step 1) obtains are introduced in the washing hypergravity swinging bed device through gas phase import, liquid phase import respectively;
In the rotor packing layer of described device, described splitting gas is drawn by gaseous phase outlet with after water contacts;
Behind the alkali lye of carrying secretly in the described water washing splitting gas, draw, to the middle circulation tank that is arranged at this device liquid phase exit, recycle by the liquid phase outlet.
2, method according to claim 1 is characterized in that: described fresh alkaline absorbent is selected from a kind of in sodium hydroxide solution, potassium hydroxide solution and the hot potassium carbonate solution or their mixture.
3, method according to claim 1 is characterized in that: described alkali cleaning step is two sections alkali cleanings, comprises the following steps:
A) splitting gas of described acid gas-containing, one section alkaline absorbent are introduced respectively in one section alkali cleaning hypergravity swinging bed device, described splitting gas is with after one section alkaline absorbent contacts in its rotor packing layer, draw by gaseous phase outlet, to two sections alkali cleaning hypergravity swinging bed devices; After described one section alkaline absorbent absorbs sour gas, drawn by the liquid phase outlet, wherein a part is drawn as waste liquid, to the liquid waste disposal district; In the circulation tank, the two sections absorption liquids of part with from two sections middle circulation tanks recycled as one section alkaline absorbent in the middle of part absorption liquid was introduced one section that is arranged at the liquid phase exit;
B) splitting gas that step a) is obtained, two sections alkaline absorbents are introduced respectively in two sections alkali cleaning hypergravity swinging bed devices, described splitting gas is with after two sections alkaline absorbents contact in its rotor packing layer, draw by gaseous phase outlet, wash to washing in the hypergravity swinging bed device; The part of described two sections absorption liquids is introduced one section as one section additional liquid; In the middle of introducing two sections that are arranged at the liquid phase exit, part absorption liquid in the circulation tank,, recycles as two sections alkaline absorbents with fresh alkaline absorbent.
4, method according to claim 3, it is characterized in that: described fresh alkaline absorbent is that mass percent concentration is the sodium hydroxide solution of 20%-30%, the mass percent concentration of sodium hydroxide is 0%-2% in one section alkaline absorbent, and the mass percent concentration of sodium hydroxide is 8%-15% in two sections alkaline absorbents.
5, method according to claim 1 is characterized in that: described alkali cleaning step is three sections alkali cleanings, comprises the following steps:
A) splitting gas of described acid gas-containing, one section alkaline absorbent are introduced respectively in one section alkali cleaning hypergravity swinging bed device, described splitting gas is with after one section alkaline absorbent contacts in its rotor packing layer, draw by gaseous phase outlet, to two sections alkali cleaning hypergravity swinging bed devices; After described one section alkaline absorbent absorbs sour gas, drawn by the liquid phase outlet, wherein a part is drawn as waste liquid, to the liquid waste disposal district; In the circulation tank, the two sections absorption liquids of part with from two sections middle circulation tanks recycled as one section alkaline absorbent in the middle of part absorption liquid was introduced one section that is arranged at the liquid phase exit;
B) splitting gas that step a) is obtained, two sections alkaline absorbents are introduced respectively in two sections alkali cleaning hypergravity swinging bed devices, described splitting gas is with after two sections alkaline absorbents contact in its rotor packing layer, draw by gaseous phase outlet, to three sections hypergravity swinging bed devices; The part of described two sections absorption liquids is introduced one section as one section additional liquid; In the circulation tank, the three sections absorption liquids of part with from three sections middle circulation tanks recycled as two sections alkaline absorbents in the middle of part absorption liquid was introduced two sections that are arranged at the liquid phase exit;
C) splitting gas that step b) is obtained, three sections alkaline absorbents are introduced respectively in three sections alkali cleaning hypergravity swinging bed devices, described splitting gas is with after three sections alkaline absorbents contact in its rotor packing layer, draw by gaseous phase outlet, wash to washing in the hypergravity swinging bed device; The part of described three sections absorption liquids is introduced two sections as two sections additional liquid; In the middle of introducing three sections that are arranged at the liquid phase exit, part absorption liquid in the circulation tank,, recycles as three sections alkaline absorbents with fresh alkaline absorbent.
6, method according to claim 5, it is characterized in that: described fresh alkaline absorbent is that mass percent concentration is the sodium hydroxide solution of 20%-30%, the mass percent concentration of sodium hydroxide is 0%-2% in one section alkaline absorbent, the mass percent concentration of sodium hydroxide is 6%-8% in two sections alkaline absorbents, and the mass percent concentration of sodium hydroxide is 12%-15% in three sections alkaline absorbents.
7, method according to claim 6 is characterized in that: the splitting gas of described acid gas-containing from five sections compressors in the cracking technology before or each section compressor outlet.
8, according to the described method of one of claim 1-7, it is characterized in that: the rotating speed of described hypergravity swinging bed device is 50-1500rpm, and the filler that uses in the described rotor packing layer is corrugated metal wire packing or waved plate butterfly filler.
9, according to the described method of one of claim 1-7, it is characterized in that: the splitting gas of described acid gas-containing is obtained by the cracking stock cracking of sulphur mass content≤0.1%.
10, a kind of method that removes the sour gas in the splitting gas is characterized in that:
At first, the splitting gas of acid gas-containing, ethanolamines solution are introduced in the hypergravity swinging bed device, in its rotor packing layer, contacted, make ethanolamines solution remove a large amount of sour gas in the described splitting gas;
Then,, adopt one of claim 1-8 described method, in hypergravity swinging bed device, carry out alkali cleaning and washing, obtain the splitting gas of content of acid gas less than 1ppm with the above-mentioned splitting gas that removes a large amount of sour gas;
The splitting gas of wherein said acid gas-containing is that the cracking stock cracking of 0.1%-0.5% obtains by the sulphur mass content.
11, method according to claim 10 is characterized in that described ethanolamines is selected from one or more in Monoethanolamine MEA BASF, diethanolamine, trolamine, methyldiethanolamine and the N methyldiethanol amine.
12, method according to claim 11 is characterized in that described ethanolamines is diethanolamine, methyldiethanolamine or N methyldiethanol amine, and its solution quality percentage concentration is 25-30%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200610086618XA CN101092576B (en) | 2006-06-23 | 2006-06-23 | Method for removing acid gases in cracked gas |
Applications Claiming Priority (1)
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