CN107866132A - SO in one kind processing Claus tail gas2Absorbing liquid and processing method - Google Patents

SO in one kind processing Claus tail gas2Absorbing liquid and processing method Download PDF

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Publication number
CN107866132A
CN107866132A CN201610855781.1A CN201610855781A CN107866132A CN 107866132 A CN107866132 A CN 107866132A CN 201610855781 A CN201610855781 A CN 201610855781A CN 107866132 A CN107866132 A CN 107866132A
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China
Prior art keywords
absorbing liquid
tail gas
amine
gas
claus tail
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CN201610855781.1A
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Chinese (zh)
Inventor
毛松柏
黄汉根
江洋洋
陈曦
汪东
郑园园
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China Petroleum and Chemical Corp
Research Institute of Sinopec Nanjing Chemical Industry Co Ltd
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China Petroleum and Chemical Corp
Research Institute of Nanjing Chemical Industry Group Co Ltd
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Priority to CN201610855781.1A priority Critical patent/CN107866132A/en
Publication of CN107866132A publication Critical patent/CN107866132A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1481—Removing sulfur dioxide or sulfur trioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/2041—Diamines

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention discloses one kind to handle SO in Claus tail gas2Absorbing liquid and its processing method, SO is removed from process gas by the absorbing liquid and processing method2, rich in SO2Absorbing liquid by steam stripping regeneration system reusable edible, purpose of the present invention is reached with this.Described absorbing liquid has the characteristics that：（1）Contain one or more reproducible organic amines in absorbing liquid；（2）Contain one or more organic amine activating agents in absorbing liquid；（3）Contain one or more organic amine reaction promoters in absorbing liquid；（4）Contain 50 ~ 88% in absorbing liquid（wt）Water.The invention also discloses SO in a set of processing Claus tail gas2Flow and device, SO can be realized by the absorbing liquid and device2Volume content is from 300 ~ 60000 mg/m3Purify to 20 mg/m3Hereinafter, the SO desorbed2Byproduct concentration is more than 99.5%.

Description

SO in one kind processing Claus tail gas2Absorbing liquid and processing method
Technical field
The invention belongs to the technical fields such as gas separation, gas purification, air environmental protection, and in particular to one kind processing Claus SO in tail gas2Absorbing liquid and method.The invention further relates to a kind of equipment for realizing this method, the equipment is included by absorbing Tower, regenerator, heat exchanger, boiling device, regeneration gas separating device, circulating pump form a set of to SO2The dress absorbed, regenerated Put, to realize recycling for absorbing liquid.
Background technology
In the industrial process such as petroleum refining and process, natural gas extraction, coal gasification preparing synthetic gas, generally produce big Amount is with hydrogen sulfide（H2S）For carbon-based sulphur of advocating peace（COS）, sulfur-bearing industrial waste gas supplemented by the organic sulfur such as mercaptan.These sulphur-containing exhaust gas In sulfide toxicity it is big, should not directly discharge, generally burn after with SO2Form be discharged into air.Developed country is to industrial mistake SO in journey2Discharge limitation, total trend is more and more severe.In the existing national atmosphere pollutants emission standardses system in China In, generality discharge performs GB16279-1996《Discharge standard of air pollutants》, special industry such as petroleum refining industry Perform《Petroleum refining industry pollutant emission standard》（Exposure draft）, thermal power plant perform GB13223-1996《Thermal power plant is big Gas pollutant emission standard》Deng.That puts into effect or revise recently from China multiple is related to SO2Knowable to the standard of discharge, industrial waste gas Middle SO2Emission concentration standard will be more and more lower, wherein GB13223-2011《Fossil-fuel power plant atmospheric pollutant emission standard》Counterweight The SO in point area2Concentration of emission has required to be less than 50mg/m3,《Petroleum refining industry pollutant emission standard》（Exposure draft） Key area is also required to be less than 100mg/m3。
Claus tail gas is the most typical industrial sulphur-containing exhaust gas of the manufacturing enterprises such as petrochemical industry, natural gas purification, coal chemical industry, And the SO of these production units discharge2One of important sources.In order to reduce the SO in discharge waste gas2Content, it is industrial frequent Using catalysis Reducing and absorption（SCOT methods）, using Catalytic Hydrogenation Techniques by the SO in Claus tail gases2, COS and CS2Deng hydrogenation or Hydrolysis is changed into H2S, again return in claus reaction device and utilize.But the investment of SCOT subtraction units is big, running cost is high, energy consumption It is high, turn into SO in long-standing problem Claus tail gas2The bottleneck for the treatment of technology, it is difficult to break through.Moreover, with national environmental protection The increasingly raising of standard, discharge flue gas can not much meet new environmental protection standard caused by existing Claus sulfur recovery technology It is required that the technological innovation replacement is imperative.Therefore, research and development other technologies turn into study hotspot.In Claus process tail gas SO2Removing can also use for reference SO in coal-fired flue-gas2Removing process.
The content of the invention
The purpose of the present invention is to be directed to SCOT subtraction units in Claus vent gas treatments to invest big, running cost height, and energy consumption occupies high The problems such as not descending, and SO in a kind of Claus tail gas proposed2Absorbing liquid and processing method.
The main technical schemes of the present invention：Contain SO in Claus tail gas2Process gas by described flow and device with Described SO2Absorbing liquid counter current contacting, absorbing and removing SO therein2, absorbing liquid passes through reusable edible after regeneration.
Absorbing liquid of the present invention includes 10 ~ 50%（wt）Organic diamine, 1 ~ 5%（wt）Organic amine activating agent, 2 ~10%（wt）Organic amine reaction promoter and 50 ~ 85%（wt）Water.
The feature of the absorbing liquid provided is：（1）Contain one or more reproducible organic amines in absorbing liquid；（2）Inhale Receive in liquid and contain one or more organic amine activating agents；（3）Contain one or more reaction promoters in absorbing liquid；（4）Absorbing liquid SO in absorbing Claus tail gas under the conditions of 20 ~ 70 DEG C of low temperature, 0.1 ~ 0.5MPa of pressure2, in 90 ~ 130 DEG C of higher temperatures, pressure By absorbing liquid steam stripping regeneration under the conditions of 0.1 ~ 0.4MPa；（5）It can be realized and recycled by the absorbing liquid after steam stripping regeneration.
SO of the present invention2In absorbing liquid, suitable total amine concentration range is 12 ~ 60%（wt）, but preferential concentration range For 20 ~ 45% (wt).
SO of the present invention2Absorbing liquid, it is 35 ~ 50 DEG C to absorb temperature range, and regeneration temperature range is 100 ~ 115 DEG C.
Organic diamine of the present invention is renewable formula organic amine, for one or more organic diamines, including ring Shape diamines etc., and in organic diamine two amine groups alkalescence it is different.
Organic amine activating agent of the present invention be hydrochloric acid, sulfuric acid, oxalic acid, acetic acid, boric acid or citric acid in one kind or It is a variety of.
Organic amine reaction promoter of the present invention is diisopropanolamine (DIPA)（DIPA）, isopropylamine base ethanol（IPAE）, isopropyl Amido isopropanol（IPAIP）, isobutyl amine ethanol（IBAE）, isobutyl amine propyl alcohol（IBAP）, isobutyl amine isopropanol （IBAIP）, tert-butylamine base propyl alcohol（TBAP）, tert-butylamine base isopropanol（TBAIP）, polyethylene glycol 400（PEG400）, ethoxy piperazine Piperazine（HEPZ）, polyethylene glycol（PEG400）, morpholine（MOR）In one or more.
One or more organic amine activating agents of the present invention, in SO2Absorbing liquid does not absorb SO2Before with it is organic The stronger amine groups of alkalescence in diamine react, generate it is stable, be difficult to the ammonium salt that regenerates；And another is alkaline Weaker amine groups, the SO in Claus tail gas is not only absorbed then with organic amine active agent response, the group2, and be SO2Absorbing liquid Adsorption equilibrium and power of regeneration, regenerating easily after heating are provided.
Described organic diamine contains 2 different amine groups of dissociation capability, has advantage on regeneration of absorption solution.Two First amine is to SO2There are good absorbent properties, in aqueous itself and SO2The process of reaction and regeneration is as follows：
First, first basic group of diamine and SO2Reaction：
（1）
Such as formula（1）Salt that is shown, being formed with the stronger amido of alkalescence, stable performance, SO2It is not easy to desorb.
Described absorbing liquid, good regenerability is provided simultaneously with, because the quality of regenerability is directly connected to absorption The re-absorption ability of agent, i.e. formula（2）Back reaction it is most important.
Diamine ion after first basic group reaction saturation continues to participate in reaction：
（2）
This process is reversible process, can inversely be carried out in the case where running into high-temperature condition, produces SO2Regeneration gas, and two after regenerating First amine aqueous solution can go successively to absorption tower and reuptake SO2, to realize recycling for absorbing liquid.
Organic amine reaction promoter of the present invention, after diamine complex role, contains SO at the same time2And CO2Deng gas Under the conditions of component, preference absorbs SO2。
SO involved in the present invention2In absorbing liquid, such as corrosion inhibiter, defoamer and similar components activating agent can also be included. The concentration range of these activating agents is 0.01% ~ 2.5%（wt）, the use of these activating agents is well known to those skilled in the art 's.
Between 3 ~ 10, pH value can control between 5 ~ 7 the pH value of absorbing liquid of the present invention.
The invention further relates to one kind to handle SO in Claus tail gas2Method, this method and described organic amine absorbing liquid one Rise and form overall technology, to realize the purpose of the present invention.
Further, SO in described processing Claus tail gas2Method, disclose SO in a set of processing Claus tail gas2's Flow and device.
Described flow comprises the following steps：
1）Claus tail gases initially enter tail gas burning furnace, and air is blasted by blower fan, at high temperature that the sulphur of various forms is complete Portion is converted into SO2；
2）Contain SO2The cooling of tail gas after incineration recovered waste heat after enter absorption tower, with organic amine absorbing liquid counter current contacting, tail SO in gas2Absorbed by organic amine absorbing liquid, the tail gas after purification directly passes through smoke stack emission；
3）Rich in SO2Absorbing liquid enter regenerator, the poor amine liquid after steam stripping regeneration through heat exchange cool down after go back to absorption tower again Recycle；
4）SO in regeneration gas2It can reach more than 99.5%（Butt, volume ratio）, high concentration SO2Regeneration gas is re-fed into Crouse Device participates in reaction production sulphur.
In technology provided by the invention, described device includes tail gas burning furnace, air blower, absorption tower, regenerator, changed The known common apparatus and tower such as hot device, boiling device, regeneration gas separating device, circulating pump；Formed in a set of tail gas to Claus SO2The generalized flowsheet and equipment absorbed, regenerated.The equipment is atmospheric pressure device, and number of devices is few, investment reduction.
SO in absorbing liquid and method processing Claus tail gas of the present invention2Concentration is 300 ~ 60000 mg/m3, desulfurization Afterwards, SO in emission2Concentration can reach 20 mg/m3Hereinafter, the SO desorbed2Byproduct concentration is more than 99.5%.
SO in Claus tail gas of the present invention2Absorbing liquid and its method compared with the handling process of SCOT methods, have Advantages below：
1）Absorbing liquid absorbability is big, and energy consumption is low, and stability is good, does not produce solid waste, small to corrosion of equipment；
2）The absorption selectivity of absorbing liquid is good, and 90% above is SO in return gas2, it is substantially free of CO2, avoid and be not involved in reacting Indifferent gas incorporation cause claus reaction stove deviate operation operating mode the problem of；
3）Device realizes recycling for absorbing liquid, operating process non-wastewater discharge；And produced in SCOT tail gas treatment process Acid water need increase sour water processing unit；
4）Device therefor is atmospheric pressure device, and number of devices is few, and process simplification is easily operated, investment reduction；
5）Normal temperature and pressure source of the gas can be handled, compared with SCOT method techniques, temperature and pressure is raised before reducing gas hydrogenation Energy consumption.
Brief description of the drawings
Fig. 1 is the simplification of flowsheet of the embodiment of the present invention.
In figure, 1- tail gas burning furnaces；2- tail gas burning furnace boilers；3- absorption towers；4- regenerators；5- boiling devices；6th, 8- is cold But device；7- poor rich liquid heat exchangers；9- regenerates gas separating device；10- burns stove air blast；11st, 12- relay pumps.
Embodiment
The present invention is illustrated by the following examples, but the present invention is not limited to following embodiments.The front and rear objective is not being departed from Scope under, change be included in the present invention technical scope in.
Embodiment is to remove SO in Claus tail gas according to amine process of the present invention2Typical technique：
Claus tail gases initially enter tail gas burning furnace, and air is blasted by blower fan, at high temperature that the sulphur of various forms is whole It is converted into SO2, contain SO2The cooling of tail gas after incineration recovered waste heat after enter absorb the bottom of the tower, and from absorption tower top spray Organic amine absorbing liquid counter current contacting under and, the SO in tail gas2Absorbed by organic amine, the tail gas after purification can directly pass through chimney Discharge.
Absorption tower is equipped with suitable column plate or filler, and the typical operation temperature in absorption tower is about at 20 ~ 70 DEG C, and pressure is about In 0.1 ~ 0.5MPa.
Rich in SO2Absorbing liquid enter regenerator by heat exchange recovery heat, poor amine liquid after steam stripping regeneration exchanges heat Absorption tower is gone back to after cooling again to recycle, high concentration SO2Regeneration gas is re-fed into Cross unit and participates in reaction production sulphur.
Regenerator is equipped with suitable column plate or filler, and for the typical operation temperature of regenerator about at 90 ~ 130 DEG C, pressure is big About in 0.1 ~ 0.4MPa.
Embodiment
Direct measurement is carried out to the operating characteristics of specific absorbing liquid and its method on an experimental rig.The absorption of experiment Tower internal diameter 50mm, the built-in porcelain Raschig rings of Φ 6 × 6 × 1, regenerator internal diameter 70mm, the built-in porcelain Raschig rings of Φ 8 × 8 × 1, regenerator Bottom is equipped with boiling device.
Certain Gas Purification Factory Claus tail gas composition is simulated, configures unstripped gas：SO2 1.10%、H2S 2.20%、CO2 3.10%、H2O 32.50%, N261.1%（It is volume ratio）.
After the completion of the configuration of organic amine absorbing liquid major constituent, the concentrated sulfuric acid 2% is successively added, then add boric acid by absorbing liquid pH value 6 or so are tuned into, remaining is deionized water.
The absorbing liquid counter current contacting that unstripped gas enters from absorb the bottom of the tower and absorption tower jacking, the acid gas in gas are absorbed, Purified gas is vented after entering the drop of gas-liquid separator recovery entrained with after being come out from tower top.
The rich solution of acid gas is absorbed to lead at the top of regenerator from absorption tower bottom, in regenerator with the steam counter-flow of rising Contact and regenerated.Lean solution after regeneration is sent into absorption tower jacking row cyclic absorption after cooling.Come out from regeneration overhead Gas enters regeneration Gas Cooler and reclaims the water vapour in gas, and regeneration gas collection after separation is handled.
Certain in gas flow, operating characteristics and the contrast of certain Gas Purification Factory operating characteristics of different absorbing liquid compositions are shown in Table one.
Embodiment 1
Certain Gas Purification Factory Claus tail gas composition is simulated, configures unstripped gas：SO2 1.10%、H2S 2.20%、CO2 3.10%、 H2O 32.50%, N261.1%（It is volume ratio）.Absorbing liquid includes 15%（wt）EDA, 5%（wt）DIPA, 2%（wt）'s Dense H2SO4, add boric acid and absorbing liquid pH value be tuned into 6 or so, remaining is deionized water.Taken off according to the invention described above amine process Except SO in Claus tail gas2Typical technique handled.The operation temperature on absorption tower is：20 DEG C, pressure is：0.1MPa；Again Giving birth to tower operation temperature is：90 DEG C, pressure is：0.1MPa.Effect is shown in Table one after purification.
Embodiment 2
Certain Gas Purification Factory Claus tail gas composition is simulated, configures unstripped gas：SO2 1.10%、H2S 2.20%、CO2 3.10%、 H2O 32.50%, N261.1%（It is volume ratio）.Absorbing liquid includes EDA20%（wt）、 DIPA8%（wt）, dense H2SO42% （wt）, add boric acid and absorbing liquid pH value be tuned into 6 or so, remaining is deionized water.Removed according to the invention described above amine process SO in Claus tail gas2Typical technique handled.The operation temperature on absorption tower is：50 DEG C, pressure is：0.25MPa；Again Giving birth to tower operation temperature is：110 DEG C, pressure is：0.2MPa.Effect is shown in Table one after purification.
Embodiment 3
Certain Gas Purification Factory Claus tail gas composition is simulated, configures unstripped gas：SO2 1.10%、H2S 2.20%、CO2 3.10%、 H2O 32.50%, N261.1%（It is volume ratio）.Absorbing liquid includes EDA15%（wt）、 PEG5%（wt）, dense H2SO42%（wt）, Absorbing liquid pH value is tuned into 6 or so by addition boric acid, and remaining is deionized water.Claus is removed according to the invention described above amine process SO in tail gas2Typical technique handled.The operation temperature on absorption tower is：70 DEG C, pressure is：0.5MPa；The regeneration Tower operation temperature is：130 DEG C, pressure is： 0.4MPa.Effect is shown in Table one after purification.
Embodiment 4
Certain Gas Purification Factory Claus tail gas composition is simulated, configures unstripped gas：SO2 1.10%、H2S 2.20%、CO2 3.10%、 H2O 32.50%, N261.1%（It is volume ratio）.Absorbing liquid includes EDA20%（wt）、PEG8%（wt）, dense H2SO42%（wt）, Absorbing liquid pH value is tuned into 6 or so by addition boric acid, and remaining is deionized water.Claus is removed according to the invention described above amine process SO in tail gas2Typical technique handled.The operation temperature on absorption tower is：35 DEG C, pressure is：0.2MPa；Regenerator is grasped It is as temperature：100 DEG C, pressure is：0.2MPa.Effect is shown in Table one after purification.
Embodiment 5
Certain Gas Purification Factory Claus tail gas composition is simulated, configures unstripped gas：SO2 1.10%、H2S 2.20%、CO2 3.10%、 H2O 32.50%, N261.1%（It is volume ratio）.Absorbing liquid includes EDA15%（wt）、HEPZ5%（wt）, dense H2SO42%（wt）, Absorbing liquid pH value is tuned into 6 or so by addition boric acid, and remaining is deionized water.Claus is removed according to the invention described above amine process SO in tail gas2Typical technique handled.The operation temperature on absorption tower is：40 DEG C, pressure is：0.25 MPa；It is described again Giving birth to tower operation temperature is：110 DEG C, pressure is：0.2 MPa.Effect is shown in Table one after purification.
Embodiment 6
Certain Gas Purification Factory Claus tail gas composition is simulated, configures unstripped gas：SO2 1.10%、H2S 2.20%、CO2 3.10%、 H2O 32.50%, N261.1%（It is volume ratio）.Absorbing liquid includes EDA 20%（wt）、HEPZ 8%（wt）, dense H2SO4 2% （wt）, add boric acid and absorbing liquid pH value be tuned into 6 or so, remaining is deionized water.Removed according to the invention described above amine process SO in Claus tail gas2Typical technique handled.The operation temperature on absorption tower is：40 DEG C, pressure is：0.25 MPa；Institute Stating regenerator operation temperature is：110 DEG C, pressure is：0.2 MPa.Effect is shown in Table one after purification.
Comparative example
Certain Gas Purification Factory Claus tail gas composition is simulated, configures unstripped gas：SO2 1.10%、H2S 2.20%、CO2 3.10%、 H2O 32.50%, N261.1%（It is volume ratio）.Using certain Gas Purification Factory SCOT method handling process.Effect is shown in after purification Table one.
One different absorbing liquids of table form to be contrasted with SCOT methods operating characteristics
The as shown by data of table one, can be by the SO in Claus tail gas using the absorbing liquid composition of the present invention2It is removed to 15mg/m3, take off Sulphur efficiency significantly improves compared with SCOT method handling process.

Claims (9)

1. SO in one kind processing Claus tail gas2Absorbing liquid, it is characterised in that the absorbing liquid include 10 ~ 50%（wt）Have Machine diamine, 1 ~ 5%（wt）Organic amine activating agent, 2 ~ 10%（wt）Organic amine reaction promoter and 50 ~ 85%（wt）Water.
2. absorbing liquid according to claim 1, it is characterised in that it is different that described organic diamine contains two alkalescence Amine groups, the stronger amine groups of its neutral and alkali are absorbing SO2Before, first generate stable ammonium with organic diamine active agent response Salt, the weaker amine groups of another alkalescence are used for SO2Absorption.
3. absorbing liquid according to claim 1, it is characterised in that described organic diamine activating agent be hydrochloric acid, sulfuric acid, One or more in oxalic acid, acetic acid, boric acid or citric acid.
4. SO according to claim 12Absorbing liquid, it is characterised in that described organic amine reaction promoter is diisopropanolamine (DIPA) （DIPA）, isopropylamine base ethanol（IPAE）, isopropylamine base isopropanol（IPAIP）, isobutyl amine ethanol（IBAE）, isobutyl amine third Alcohol（IBAP）, isobutyl amine isopropanol（IBAIP）, tert-butylamine base propyl alcohol（TBAP）, tert-butylamine base isopropanol（TBAIP）, poly- second Glycol 400（PEG400）, hydroxyethyl piperazine（HEPZ）, polyethylene glycol（PEG400）, morpholine（MOR）In one or more.
5. absorbing liquid according to claim 1, it is characterised in that total amine concentration is 12 ~ 60% in the absorbing liquid（wt）.
6. absorbing liquid according to claim 1, it is characterised in that it is 0.01 ~ 2.5% that concentration range is added in the absorbing liquid （wt）Corrosion inhibiter, defoamer.
7. absorbing liquid according to claim 1, it is characterised in that the pH value of the absorbing liquid is controlled between 3-10.
A kind of 8. SO in any described absorbing liquid processing Claus tail gas using claim 1-82Method, it is characterised in that bag Include following steps：
1）Claus tail gas initially enters tail gas burning furnace, and the sulphur of various forms is converted into SO at high temperature2；
2）Contain SO2Tail gas after incineration enter absorption tower after cooling, and absorbing liquid counter current contacting, the SO in tail gas2Absorbed Liquid is absorbed, and the tail gas after purification can be discharged directly；
3）Rich in SO2Absorbing liquid enter regenerator, the poor amine liquid after steam stripping regeneration through heat exchange cool down after return absorption tower follow Ring utilizes；
4）SO in regeneration gas2Butt, volume ratio reach more than 99.5%, high concentration SO2Regeneration gas is re-fed into Cross unit Participate in reaction production sulphur.
9. according to the method for claim 9, it is characterised in that：The operation temperature on the absorption tower is：20 ~ 70 DEG C, pressure For：0.1~0.5MPa；The regenerator operation temperature is：90 ~ 130 DEG C, pressure is：0.1~0.4MPa.
CN201610855781.1A 2016-09-28 2016-09-28 SO in one kind processing Claus tail gas2Absorbing liquid and processing method Pending CN107866132A (en)

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Application publication date: 20180403