CN106608618A - Acid gas purification process - Google Patents
Acid gas purification process Download PDFInfo
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- CN106608618A CN106608618A CN201510685583.0A CN201510685583A CN106608618A CN 106608618 A CN106608618 A CN 106608618A CN 201510685583 A CN201510685583 A CN 201510685583A CN 106608618 A CN106608618 A CN 106608618A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0415—Purification by absorption in liquids
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/146—At least two purification steps in series
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Abstract
The present invention relates to an acid gas purification process, which is a combination process comprising pre-washing with low temperature methanol washing, tandem pre-washing regeneration and room temperature composite solvent desulfurization, decarburization and rich liquid regeneration, wherein the absorbent is a composite solvent and comprises, by weight, 40-55 parts of methanol and 30-45 parts of hindered amine, the total sulfur in the crude synthesis gas can be removed to achieve less than 1 ppm and CO2 can be removed to less than 20 ppm with the composite solvent, and the hindered amine is added and has a chemical absorption effect, such that the operation of the method cannot be performed at the low temperature. Compared to the conventional low temperature methanol washing process, the process of the present invention has the following advantages that the disadvantages of high cold-energy consumption, high investment caused by the use of the low temperature material, the low temperature pump, the low temperature pipe, the valve and the like, and high energy consumption of the low temperature methanol washing are solved, the disadvantage of easy degradation of the common room temperature methanol washing solvent is solved, and the acid gas purification process can be used for the industrial application of acid gas purification.
Description
Technical field
The present invention relates to a kind of acid gas purification technique.
Background technology
H is contained by coal gasification production by raw material of coal2With the crude synthesis gas of CO, then by synthesis gas downstream product such as
Synthesis ammonia, methanol, dimethyl ether, hydrogen, alkene, artificial oil, IGCC generatings etc. are the main skills of China's energy substitution
Art route.Using in the crude synthesis gas that coal gasifying process is produced except containing CO, H2、CO2Outward, also a small amount of H2S、
COS、CH4、N2And the composition such as micro chlorine, ammonia, synthesis gas need to be purified to meet downstream production requirement.
From the point of view of purification technique employed in domestic and international coal gasification apparatus, it is most suitable in current purification techniques that low-temp methanol is washed
Close the gas purifying technique of extensive Development of Coal Chemical Industry.The technique with low-temp methanol as lyosoption, using methanol in low temperature
Under to the great good characteristic of sour gas dissolubility, the sour gas in unstripped gas is removed using Physical Absorption.The process gas
Degree of purification is high, and selectivity is good, and gas sweetening, decarburization can be segmented in same tower, optionally carry out, and H2S's
Dissolubility compares CO2Dissolubility it is much bigger, it is possible to achieve selectively remove H2S, final recyclable sulfur.
At present abroad operation of putting into production, particularly 20 century 70s are put in existing nearly hundred sets of low temperature methanol cleanings makeup
Start, the Mass Synthetic Ammonia Unit with coal and heavy oil as raw material that foreign countries are built is mostly using the purification technique removing sour gas
Body.The low-temp methanol washing process flow process of LURGI is gasification-desulfurization-conversion-decarburization, is converted between desulfurization and decarburization,
And the low-temp methanol washing process of Linde Co is then selective one-step method desulfurization and decarburization after conversion.As low-temp methanol washes work
The extensive application in industrialized unit of skill, opens again for different raw material and gasification process, LURGI and Linde Co
Have issued kinds of processes flow process makes the in hgher efficiency of whole flow process, and energy utilization is more abundant and reasonable.But, using low
Warm methanol cleaning must consume a large amount of colds, using low temperature material Tu, cryopump, low temperature pipe fitting and valve etc., invest phase
Should increase, energy consumption increases, therefore, bring difficulty to the popularization and application that low-temp methanol is washed.
In recent years, the room temperature methanol for growing up on the basis of low-temp methanol is washed is washed, and is to add to fit as basic solvent with methanol
The alkanolamine (such as Amisol plus ethanolamine) of amount and water composition mixed solvent, this solvent is with physical dissolution and chemical absorbing
Effect.And the method can be without cryogenic material, pump, pipe fitting and under conditions of not consuming cold substantially, by gas under isothermal
Body high purification (purified gas total sulfur<Lppm, CO2<50ppm).The shortcoming of MEA is easily foaming and degrades rotten.
CO in purification process in MEA and unstripped gas2Side reaction can occur and generate and be difficult to the drops such as regeneration degraded Evil seat alkanones
Solution product, causes partial solvent to lose decarburization capacity.Meanwhile, the regeneration temperature of MEA is higher, regenerates column bottom temperature one
As more than 121 DEG C, cause under regenerative system seriously corroded, then peracidity gas load then more very.Therefore, MEA is molten
The mass fraction of liquid typically adopts 15%, and highest is also less than 20%；And sour gas load also only takes 0.3moL acid gas/mol
Hydramine or so.DEA is secondary alcohol amine, it and CO compared with MEA2Reaction rate it is lower, therefore occur side reaction and make
Into solvent loss amount it is relatively fewer.In reasonable selection material and using in the case of corrosion inhibiter, the matter of DEA aqueous solutions
Amount fraction can be improved to 55%, and sour gas load also can reach more than 0.7mol acid gas/mol hydramine, so as to significantly drop
Low solution circulating load, and degree of purification also makes moderate progress.
Room temperature methanol washes the gaseous light oil that solvent can be absorbed in lurgi pressure gasification gas, but the regeneration of prewashing rich solution and light
The extraction of oil can encounter new problem, and lack ripe practice.In addition room temperature methanol washes depositing due to alkanolamine in solvent
Can be with some of unstripped gas impurity or gaseous component (such as CO2, COS, HCN) reacting causes chemical degradation.
Therefore, current ambient temperature methanol is washed and still have in terms of theory and practice certain limitation.
The limitation of prewashing gaseous light oil is washed for room temperature methanol, set forth herein using formula solvent, the solvent includes first
Alcohol and bulky amine, with the group that low-temp methanol washes prewashing, prewashing regeneration string room temperature double solventss desulfurization, decarburization and rich solution regeneration
Interflow journey.
New acid gas purification technique is divided into two parts gas purification.Prewashing and prewashing regeneration technology are washed using low-temp methanol,
Relatively easily removed gaseous light oil.And room temperature double solventss desulfurization, the advantage of decarburization can be relied on, by gas
Body obtains high purification.
The content of the invention
The technical problem to be solved is that the purification process energy consumption of acid gas present in prior art is high, degree of purification is low,
The problems such as solvent is unstable, there is provided a kind of new acid gas purification technique, when the technique is purified for acid gas, with investment
Less, the advantages of energy consumption is low, degree of purification is high, solvent stability is not degradable by force.
For achieving the above object, the present invention takes technical scheme below：A kind of acid gas purification technique, comprises the steps：
Crude synthesis gas cooling, desulfurization, decarburization, the regeneration of methanol prewashing rich solution, the essence regeneration of methanol rich solution, methanol-water separation, tail
Gas washing, it is characterised in that：Elder generation Jing low-temp methanol prewashing operations before (a) desulfurization and decarburization, it is (b) main to wash absorbent used by tower
Using double solventss, double solventss main component includes methanol and bulky amine.
In above-mentioned technical proposal, it is preferable that double solventss include methanol and bulky amine, in terms of parts by weight, methanol content
For 40-55 parts, steric hindrance amine content is 30-45 parts.
In above-mentioned technical proposal, it is preferable that also contain water in double solventss.
In above-mentioned technical proposal, it is preferable that technological process adds the technological process that double solventss master washes using low-temp methanol prewashing.
In above-mentioned technical proposal, it is preferable that low-temp methanol prewashing process operation temperatures are -20～-55 DEG C, more preferably
- 25 DEG C～-35 DEG C.
In above-mentioned technical proposal, it is preferable that the amount of allocating of low-temp methanol prewashing is 4-10kg/1000Nm3；It is highly preferred that
The amount of allocating of low-temp methanol prewashing is 5-8kg/1000Nm3
In above-mentioned technical proposal, it is preferable that master washes process operation temperatures for 0-25 DEG C；It is highly preferred that master washes technological operation
Temperature is 10-20 DEG C.
In above-mentioned technical proposal, it is preferable that column plate used by absorption tower is eddy flow solid valve, eddy flow float valve combined column plate.
In above-mentioned technical proposal, it is preferable that open ratio of plate used by absorption tower is 5%-20%.
In above-mentioned technical proposal, it is preferable that column plate valve opening gas phase loading factor opereating specification used by absorption tower is 5-20.
In above-mentioned technical proposal, it is preferable that absorption tower void tower gas phase loading factor opereating specification is 0.1-3.5.
Acid gas removing is carried out using above-mentioned technical proposal, detailed technological process is as follows：
(a) crude synthesis gas cooling stage：The crude synthesis gas of about 40 DEG C sent from synthesis gas conversion section are in the first heat exchange
Device (1) exchanges heat, and crude synthesis gas are cooled to+8 DEG C and prevent from freezing with methanol spray Jing after gas-liquid separation (2), slightly synthesize thereafter
Gas Jing exchanges heat or Jing ammonia coolers (3) are further cooled to -25 DEG C to enter prewashing section.The cold prewashing gas Jing of prewashing outlet is slightly closed
Reclaim after cold into gas second heat exchanger, sending into absorption tower (5) at about 20 DEG C or so carries out desulfurization, decarburization.
(b) prewashing and desulfurization, decarburization：The low-temp methanol counter current contacting that crude synthesis gas are sprayed on prewashing section and top, it is contained
Gaseous light oil, moisture and part organic sulfur here are dissolved and absorb.After go out prewashing section cryogenic gas in coal gas cooling end
Divide and enter feeding master after workshop section's crude synthesis gas countercurrent flow recovery cold and wash tower.Tower gas is washed in master to contact with double solventss,
The total sulfur in purified gas is set to be less than lppm, CO2Less than 20ppm.
The regeneration of (c) methanol prewashing rich solution：After going out prewashing section, prewashing methanol rich solution feed turntable extraction tower extraction Jing after vacuum flashing
Take light oil.A certain amount of washings come by regenerator and water scrubber are respectively fed on turntable extracting tower top and top, and
The soft water sent by full factory's soft water system makees light oil extractant.The light oil for extracting sends workshop section as product.
Raffinate autorotation disk extraction tower bottom is discharged and sends into methanol-water rectifying column.The methanol steam of tower top rectification as essence again
The thermal source of raw tower reboiler, goes out the methanol gas-liquid mixture Jing refrigerated separations of reboiler, and major part condensation methanol is used as rectification
Tower backflow, extracts a certain amount of methanol and is pumped up toward prewashing section as prewashing recycle methanol.Ammonia is set before prewashing section is entered
Cooler, to cool down to prewashing methanol.
In addition to blowdown being needed according to systematic water balance and send biochemical treatment part, remaining returns regeneration gas washing to rectifying column bottom waste water
Section middle part, in washing, reclaiming gas after active component, send extraction water system circulation to use.
The regeneration of (d) room temperature double solventss rich solution：The room temperature double solventss that master washes tower are sent into, after receipts have inhaled acidic components
Section bottom is washed by master to draw, Jing vacuum flashings first, send in regenerator regenerate thereafter.
Compared with prior art, the present invention has advantages below：(1) solve low temperature methanol cleaning cold and consume big,
Big, the shortcoming of high energy consumption using investment caused by low temperature material Tu, cryopump, low temperature pipe fitting and valve etc.；(2) while solution
Common room temperature methanol of having determined washes the degradable shortcoming of solvent.
The specific embodiment of the invention is further described with reference to Figure of description.
Description of the drawings
Fig. 1 is acid gas purification process chart.
(1) First Heat Exchanger, (2) gas-liquid separation, (3) ammonia cooler, (4) second heat exchangers, (5) absorption tower, (6)
Flash column, (7) regenerator, (8) the 3rd heat exchangers, (A) crude synthesis gas, (B) purified gas, (C) CO2, (D) H2S
As shown in figure 1, the crude synthesis gas A sent from conversion section exchanges heat in first heat exchanger (1), crude synthesis gas quilt
Cooling prevents from freezing Jing after gas-liquid separation (2) with methanol spray, and thereafter crude synthesis gas Jing ammonia coolers (3) further cool down laggard
Enter absorption tower (5) prewashing section.Prewashing outlet cold prewashing gas Jing crude synthesis gas second heat exchanger (4) reclaim cold after,
Feeding absorption tower (5) master washes section carries out desulfurization, decarburization.
Crude synthesis gas in absorption tower (5) prewashing section and the low-temp methanol counter current contacting of top spray, contained gaseous light oil,
Moisture and part organic sulfur here are dissolved and absorb.After go out prewashing section cryogenic gas synthesis gas cooling segment with enter workshop section
Crude synthesis gas countercurrent flow reclaims feeding master after cold and washes section.Section gas and the room temperature double solventss from regenerator are washed in master
Counter current contacting, makes the H in crude synthesis gas2S、CO2Absorb in the section.Total sulfur in control purified gas B is less than lppm,
CO2 is less than 20ppm.
After going out prewashing section, prewashing methanol rich solution feed turntable extraction tower extraction light oil Jing after vacuum flashing.On turntable extracting tower
Portion and top are respectively fed to a certain amount of washings come by regenerator and water scrubber, and by full factory's soft water system send it is soft
Water makees light oil extractant.The light oil for extracting sends workshop section as product.
Raffinate autorotation disk extraction tower bottom is discharged and sends into methanol-water separating.The methanol steam of tower top rectification as essence again
The thermal source of raw tower reboiler, goes out the methanol gas-liquid mixture Jing refrigerated separations of reboiler, and major part condensation methanol is used as methanol
Water separation column backflow, extracts a certain amount of methanol and is pumped up toward prewashing section as prewashing recycle methanol.Before prewashing section is entered
Ammonia cooler is set, to cool down to prewashing methanol.
In addition to blowdown being needed according to systematic water balance and send biochemical treatment part, remaining is returned again methanol-water separating tower bottom waste water
Anger washing tower section middle part, in washing, reclaiming gas after active component, send extraction water system circulation to use.
The room temperature double solventss on absorption tower are sent into, section bottom is washed by master after receipts have inhaled acidic components and is drawn, the decompressions of Jing first
Flash column (6), regenerator (7) is sent into after it Jing after the heat exchange of the 3rd heat exchanger (8).To press from both sides in thorough reclaiming gas
The methanol and bulky amine droplet and steam of band, regeneration gas water scrubber bottom with methanol-water separating come waste water wash,
Regeneration gas water scrubber top again with flash steam washing section come soft water regenerated from washing gas.
Specific embodiment
【Embodiment 1】
Production scale is 115 × 104Nm3/ h crude synthesis gas, need to process conversion tolerance：9×104Nm3/h。
The composition of conversion gas such as table 1：(vol%)
Table 1
| CO2 | CO | H2 | N2 | CH4 | HCN | H2S |
| 43.529 | 0.323 | 55.23 | 0.352 | 0.024 | 0.002 | 0.188 |
Using acid gas purification technique, the technique includes crude synthesis gas cooling, prewashing and desulfurization, decarburization, prewashing rich solution again
The raw, regeneration of double solventss rich solution.Wherein double solventss are made up of methanol and bulky amine, and by weight, methanol content is
55 parts, steric hindrance amine content is 30 parts, and remaining is water.Technological process adds what double solventss master washed using low-temp methanol prewashing
Technological process.Low-temp methanol prewashing process operation temperatures are -25 DEG C.The amount of allocating of low-temp methanol prewashing is 5kg/1000Nm3,
Master washes process operation temperatures for 20 DEG C, and column plate used by absorption tower is eddy flow solid valve, eddy flow float valve combined column plate.
Concrete technology flow process is as follows：
The crude synthesis gas A of about 40 DEG C sent from conversion section exchanges heat in first heat exchanger (1), and thick synthesis A gas is cold
But prevent from freezing with methanol spray Jing after gas-liquid separation (2) to 8 DEG C, thereafter crude synthesis gas Jing Jing ammonia coolers (3) are further cooled down
Prewashing section is entered to -25 DEG C.Prewashing outlet cold prewashing gas Jing crude synthesis gas second heat exchanger (4) reclaim cold after,
Sending into absorption tower (5) at about 20 DEG C or so carries out desulfurization, decarburization.
Crude synthesis gas A is in absorption tower (5) prewashing section and the low-temp methanol counter current contacting of top spray, contained gaseous light
Oil, moisture and part organic sulfur here are dissolved and absorb.After go out prewashing section cryogenic gas synthesis gas cooling segment with enter
Workshop section's crude synthesis gas countercurrent flow reclaims feeding master after cold and washes section.Section gas is washed in master to be combined with the room temperature from regenerator
Solvent counter current is contacted, and makes the H in crude synthesis gas2S、CO2Absorb in the section.Total sulfur in control purified gas B is less than lppm,
CO2Less than 20ppm.
Subsequent treatment process includes the works such as the regeneration of prewashing methanol rich solution, methanol-water separation, double solventss regeneration and vent gas treatment
Sequence, its brief technological process is as follows：
After going out prewashing section, prewashing methanol rich solution feed turntable extraction tower extraction light oil Jing after vacuum flashing.On turntable extracting tower
Portion and top are respectively fed to a certain amount of washings come by regenerator and water scrubber, and by full factory's soft water system send it is soft
Water makees light oil extractant.The light oil for extracting sends workshop section as product.
Raffinate autorotation disk extraction tower bottom is discharged and sends into methanol-water separating.The methanol steam of tower top rectification as essence again
The thermal source of raw tower reboiler, goes out the methanol gas-liquid mixture Jing refrigerated separations of reboiler, and major part condensation methanol is used as methanol
Water separation column backflow, extracts a certain amount of methanol and is pumped up toward prewashing section as prewashing recycle methanol.Before prewashing section is entered
Ammonia cooler (3) is set, to cool down to prewashing methanol.
In addition to blowdown being needed according to systematic water balance and send biochemical treatment part, remaining is returned again methanol-water separating tower bottom waste water
Anger washing tower section middle part, in washing, reclaiming gas after active component, send extraction water system circulation to use.
The room temperature double solventss on absorption tower are sent into, section bottom is washed by master after receipts have inhaled acidic components and is drawn, the decompressions of Jing first
Flash column (6), is then fed into regenerator (7).Wherein account for the solution of global cycle amount 90%, the heat exchangers (8) of Jing the 3rd
It is heated to about 75 DEG C and enters regenerator middle part, sends at the top of regenerator at 35 DEG C or so after about 10% solution is water cooled.
Reboiler thermal source is supplied by low-pressure steam.
For in thorough reclaiming gas carry secretly methanol and bulky amine droplet and steam, in regeneration gas water scrubber bottom methanol
Water separation column come waste water washing, regeneration gas water scrubber top again with flash steam washing section come soft water regenerated from washing gas.
The process stabilizing runs 72 hours, and total sulfur is less than 1ppm, CO in synthesis gas after purification2Under meeting less than 20ppm
Trip technic index.
【Embodiment 2】
Unstripped gas composition, technological process with【Embodiment 1】It is identical including crude synthesis gas cooling, prewashing and desulfurization, de-
Carbon, the regeneration of prewashing rich solution, the regeneration of double solventss rich solution.Wherein double solventss are made up of methanol and bulky amine, with weight
Gauge, methanol content is 45 parts, and steric hindrance amine content is 40 parts, and remaining is water.Technological process adopts low-temp methanol prewashing
Plus the technological process that double solventss master washes.Low-temp methanol prewashing process operation temperatures are -35 DEG C.Low-temp methanol prewashing is matched somebody with somebody
Enter amount for 8kg/1000Nm3, it is 10 DEG C that master washes process operation temperatures, and column plate used by absorption tower is that admittedly valve, eddy flow are floated eddy flow
Valve combined column plate.
The process stabilizing runs 72 hours, and total sulfur is less than 1ppm, CO in synthesis gas after purification2Under meeting less than 20ppm
Trip technic index.
【Embodiment 3】
Unstripped gas composition, technological process with【Embodiment 1】It is identical including crude synthesis gas cooling, prewashing and desulfurization, de-
Carbon, the regeneration of prewashing rich solution, the regeneration of double solventss rich solution.Wherein double solventss are made up of methanol and bulky amine, with weight
Gauge, methanol content is 40 parts, and steric hindrance amine content is 45 parts, and remaining is water.Technological process adopts low-temp methanol prewashing
Plus the technological process that double solventss master washes.Low-temp methanol prewashing process operation temperatures are -40 DEG C.Low-temp methanol prewashing is matched somebody with somebody
Enter amount for 8kg/1000Nm3, it is 5 DEG C that master washes process operation temperatures, and column plate used by absorption tower is that admittedly valve, eddy flow are floated eddy flow
Valve combined column plate.
The process stabilizing runs 72 hours, and total sulfur is less than 1ppm, CO in synthesis gas after purification2Under meeting less than 20ppm
Trip technic index.
【Comparative example 1】
Using low-temp methanol washing process, synthesis gas composition is same as Example 1.Equally, it is net through low-temp methanol washing process
After change, total sulfur is less than 1ppm, CO in synthesis gas after purification2Meet downstream process index less than 20ppm.Together【Implement
Example 1】Compare, the two observable index relatively the results are shown in Table 2.
Table 2
【Comparative example 2】
Using other room temperature methanol cleaning process, using double solventss：60% methanol, 38% diethanolamine, 2% water are as suction
Solvent is received, it is 35 DEG C to absorb temperature, and 85 DEG C of regeneration temperature, synthesis gas composition is same as Example 1.Equally, pass through
After the technique room temperature methanol cleaning process purification, total sulfur is less than 1ppm, CO in synthesis gas after purification2Meet less than 20ppm
Downstream process index, and energy consumption index is same【Embodiment 3】It is close to.But have that operating flexibility is little, pipeline is easily blocked,
The shortcomings of total sulfur is easily exceeded, solution consumption amount is big.
This technique in terms of investment, cost and energy consumption is can be seen that from above comparing result to wash compared with low-temp methanol and contrast
Room temperature methanol cleaning process flow process has larger superiority in example.
Claims (10)
1. a kind of acid gas purification technique, comprises the steps：Crude synthesis gas cooling, desulfurization, decarburization, methanol prewashing rich solution
Regeneration, methanol rich solution essence regeneration, methanol-water separate, washing tail gas, it is characterised in that：(a) desulfurization and decarburization
Elder generation Jing low-temp methanol prewashing operations before, (b) master wash absorbent used by tower and adopt double solventss, double solventss
Including methanol and bulky amine.
2. acid gas purification technique according to claim 1, it is characterised in that technological process adds for low-temp methanol prewashing
The technological process that double solventss master washes.
3. acid gas purification technique according to claim 1, it is characterised in that absorbent used by acid gas purification technique is
Double solventss, double solventss include methanol and bulky amine, and methanol content is counted as 40-55 parts with parts by weight,
Steric hindrance amine content is 30-45 parts.
4. acid gas purification technique according to claim 1, it is characterised in that low-temp methanol prewashing process operation temperatures
For -20～-55 DEG C.
5. acid gas purification technique according to claim 1, it is characterised in that the master washes process operation temperatures and is
0-25℃。
6. acid gas purification technique according to claim 1, it is characterised in that the amount of allocating of the low-temp methanol prewashing
For 4-10kg/1000Nm3。
7. acid gas purification technique according to claim 1, it is characterised in that column plate used by described absorption tower is rotation
The solid valve of stream and eddy flow float valve combined column plate.
8. acid gas purification technique according to claim 1, it is characterised in that column plate perforate used by described absorption tower
Rate is 5%-20%.
9. acid gas purification technique according to claim 1, it is characterised in that column plate valve opening used by described absorption tower
Gas phase loading factor opereating specification is 5-20.
10. acid gas purification technique according to claim 1, it is characterised in that described absorption tower void tower gas phase is moved
Energy factor opereating specification is 0.1-3.5.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4101633A (en) * | 1977-02-14 | 1978-07-18 | Exxon Research & Engineering Co. | Process and composition for removing carbon dioxide containing acidic gases from gaseous mixtures |
| CA2736222A1 (en) * | 2008-10-14 | 2010-04-22 | Exxonmobil Upstream Research Company | Removal of acid gases from a gas stream |
| CA2683094A1 (en) * | 2009-04-30 | 2010-10-30 | Mitsubishi Heavy Industries, Ltd. | Method and apparatus for separating acidic gases from syngas |
| CN101874967A (en) * | 2009-12-18 | 2010-11-03 | 中国五环工程有限公司 | Process for removing acid gas with low-temperature methanol solution |
| CN101885993A (en) * | 2010-07-12 | 2010-11-17 | 赛鼎工程有限公司 | Purification process for removing sulphur and carbon dioxide in gas by using two-step method |
| CA2777760A1 (en) * | 2009-11-02 | 2011-05-05 | Exxonmobil Upstream Research Company | Cryogenic system for removing acid gases from a hydrocarbon gas stream, with removal of hydrogen sulfide |
| CN102806000A (en) * | 2012-09-05 | 2012-12-05 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step rectisol method |
| CN203139876U (en) * | 2012-12-26 | 2013-08-21 | 新奥科技发展有限公司 | Low-temperature methanol washing process device |
| CN203639435U (en) * | 2013-12-20 | 2014-06-11 | 上海国际化建工程咨询公司 | Device for combining normal temperature/low temperature methanol washing to process crude synthesis gas containing oil |
| WO2014129254A1 (en) * | 2013-02-21 | 2014-08-28 | 三菱重工業株式会社 | System and method for recovering gas containing co2 and h2s |
-
2015
- 2015-10-21 CN CN201510685583.0A patent/CN106608618A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4101633A (en) * | 1977-02-14 | 1978-07-18 | Exxon Research & Engineering Co. | Process and composition for removing carbon dioxide containing acidic gases from gaseous mixtures |
| CA2736222A1 (en) * | 2008-10-14 | 2010-04-22 | Exxonmobil Upstream Research Company | Removal of acid gases from a gas stream |
| CA2683094A1 (en) * | 2009-04-30 | 2010-10-30 | Mitsubishi Heavy Industries, Ltd. | Method and apparatus for separating acidic gases from syngas |
| CA2777760A1 (en) * | 2009-11-02 | 2011-05-05 | Exxonmobil Upstream Research Company | Cryogenic system for removing acid gases from a hydrocarbon gas stream, with removal of hydrogen sulfide |
| CN101874967A (en) * | 2009-12-18 | 2010-11-03 | 中国五环工程有限公司 | Process for removing acid gas with low-temperature methanol solution |
| CN101885993A (en) * | 2010-07-12 | 2010-11-17 | 赛鼎工程有限公司 | Purification process for removing sulphur and carbon dioxide in gas by using two-step method |
| CN102806000A (en) * | 2012-09-05 | 2012-12-05 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step rectisol method |
| CN203139876U (en) * | 2012-12-26 | 2013-08-21 | 新奥科技发展有限公司 | Low-temperature methanol washing process device |
| WO2014129254A1 (en) * | 2013-02-21 | 2014-08-28 | 三菱重工業株式会社 | System and method for recovering gas containing co2 and h2s |
| CN203639435U (en) * | 2013-12-20 | 2014-06-11 | 上海国际化建工程咨询公司 | Device for combining normal temperature/low temperature methanol washing to process crude synthesis gas containing oil |
Non-Patent Citations (4)
| Title |
|---|
| 王之德: "位阻胺脱硫脱碳工艺及其进展", 《天然气化工》 * |
| 王开岳: "《天然气净化工艺 脱硫脱碳、脱水、硫磺回收及尾气处理》", 31 July 2005, 石油工业出版社 * |
| 王骏: "用"改良常温甲醇洗"代低温甲醇洗净化鲁奇加压气化气的探讨", 《煤化工》 * |
| 蔡必楷 等编著: "《化工原理程序设计》", 30 September 1994, 山西高校联合出版社 * |
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