CN109529567A - A kind of technique of hydrogen sulfide and sulfur dioxide reaction desulfuration - Google Patents

A kind of technique of hydrogen sulfide and sulfur dioxide reaction desulfuration Download PDF

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Publication number
CN109529567A
CN109529567A CN201710857887.XA CN201710857887A CN109529567A CN 109529567 A CN109529567 A CN 109529567A CN 201710857887 A CN201710857887 A CN 201710857887A CN 109529567 A CN109529567 A CN 109529567A
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reaction
gas
hydrogen sulfide
reactor
basic compound
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CN109529567B (en
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李磊
李欣
王海波
金平
齐慧敏
韩天竹
王昊辰
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Sinopec Dalian Petrochemical Research Institute Co ltd
China Petroleum and Chemical Corp
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China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
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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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/52—Hydrogen sulfide
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/05—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by wet processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity

Abstract

A kind of technique of hydrogen sulfide and sulfur dioxide reaction desulfuration, including the following contents: hydrogen sulfide containing gas and the gas containing sulfur dioxide are passed through reactor, reactor is provided with reaction solution, the reaction solution includes water and at least one organic basic compound miscible with water, and the organic basic compound makes pH value >=7.2 of the solution；Hydrogen sulfide is reacted with sulfur dioxide generates sulphur, during the reaction takes out sulphur, and supplement reaction solution online, or to after reaction separate the liquid in reactor admittedly, obtain sulphur.The addition of organic basic compound makes H in technology utilization reaction solution of the invention2S and SO2Reaction time in the liquid phase greatly shortens, and the reaction response time is lower than 15 seconds, and the desulfurization that can react under normal temperature and pressure.Only the sulphur of high-purity need to can be obtained, reaction condition needed for technique of the invention is mild, the simple easy processing of equipment, low investment, safe operation by simple solid-liquor separation without purification.

Description

A kind of technique of hydrogen sulfide and sulfur dioxide reaction desulfuration
Technical field
The present invention relates to a kind of techniques for hydrogen sulfide and sulfur dioxide reaction desulfuration, belong to industrial production or Industry Waste Gas field of purification.
Background technique
It due to China's expanding economy, is growing on and on to the demand of crude oil, domestic crude oil has been insufficient for its people Demand, so just continually input is Chinese for imported crude oil.The 1-12 month in 2016 China 381,010,000 tons of imported crude oil, with last year The same period is compared to growth by 13.6%.With the increase year by year of China's imported crude oil amount, specific gravity shared by high-sulphur crude is increasing, Major oil refining enterprise develops a series of high sulfur bauxite technique thus, sour crude in hydrofinishing, be hydrocracked, urge Change to generate in the process such as cracking and largely contains H2S sour gas and contain SO2Flue gas.
For containing SO2The processing of flue gas be divided into dry method, semidry method and three kinds of wet process, wet desulphurization at present has desulfurization degree It is high, device is reliable for operation, simple operation and other advantages, thus the existing flue gas desulfurization technique in countries in the world is mainly with wet desulphurization It is main.Traditional Wet Flue Gas Desulfurization Technique mainly has limestone-gypsum method, double alkali method desulfurizing, sodium alkali desulfurization, ammonia process of desulfurization method etc..
For containing H2The processing of S sour gas, it is industrial at present it is more commonly used there are two types of recovery technologies, one is uses Fixed bed catalytic oxidation, most common method are claus process；Another kind is U.S. Merichem company gas technology product The LO-CAT technique of company (GTP) exploitation.
Traditional Cross unit is made of a high temperature section and two or three conversion zones.High temperature section includes H2S combustion furnace And waste heat boiler, Claus method are to utilize the H in gas2S makes H in Crouse's combustion furnace2S portion oxidation generates SO2, burning Reaction equation is H2S+1.5O2→SO2+H2O, there are about 1/3 H2S is anti-in combustion furnace with air at a temperature of 1200 DEG C or so SO should be generated2, remaining unreacted H2The same SO of S2Claus reaction is continued to complete by means of catalyst in the lower conversion zone of temperature Generate sulphur.Reaction equation in Claus conversion device is 2H2S+SO2→3S+2H2O。
The reaction process of LO-CAT technique carries out in a kind of weakly alkaline liquid-phase system, will using chelating iron catalyst H2S is converted into elemental sulfur.Its reaction principle are as follows: H2After S gas is dissolved in water, it is ionized into H+And HS-: H2S→H++HS-.In solution Catalyst Fe3+With HS-Redox reaction, HS occurs-It is converted to elemental sulfur, Fe3+Then it is reduced to Fe2+: HS-+2Fe3+→ S+2Fe2++H+.The technique uses the regenerating medium of air (oxygen) as iron catalyst, by Fe2+It is oxidized to Fe3+, make catalyst Activity recovery, process are as follows: 2Fe2++1/2O2+H2O→2Fe3++2OH-.Total chemical equation are as follows: H2S+1/2O2→S+ H2O
LO-CAT technique can only be handled containing H2The sour gas of S, by H2S is converted into elemental sulfur.After claus process and various improvement Claus process to H in unstripped gas2S content requires, H in unstripped gas2S content will at least reach 10% or more, if raw material H in gas2S content is lower, needs to enter Cross unit after concentrate is handled；At method of the claus process using burning Reason contains H2The sour gas of S, thus gas to be processed cannot directly enter Crouse's combustion furnace if having combustibility, it is necessary to The techniques such as amine purification are first passed through by H2S removes out subsequently into claus oven；Claus process need to first make H2S portion oxidation life At SO2Then the two reaction generates sulphur, since claus process desulfuration efficiency is limited, needs more reactor tandems reactions, instead Answer temperature higher；As environment protection emission index is more and more harsher, it is necessary to which mating claus tail-gas clean-up device is wanted with meeting environmental protection It asks.In addition, LO-CAT technique and claus process can only be handled containing H2The sour gas of S is difficult to handle H simultaneously2S gas and SO2 Gas, for the deficiency of two kinds of technique, developing some can be handled simultaneously containing H2S and SO2The technique of gas.
JGC Corporation discloses a kind of Crouse carried out in the pure water without any additive in CN86101352 Reaction, the H when the pH value of aqueous medium in reactor is lower than 22S and SO2The reaction that liquid phase generates sulphur is the strongest, thus uses Reaction pressure > 5kg/cm2Liquid-phase claus reaction Recovered sulphur is carried out under conditions of (gauge pressure), pH value<2, temperature>120 DEG C.
CN201310546164.X discloses a kind of side for using water mist and water vapour as catalyst treatment hydrogen sulfide gas Method makes H using water mist and water vapour as catalyst2S and SO2It reacts, optimal reaction temperature is 50 ~ 60 DEG C, and sulphur turns Rate can reach 90% or so.
CN201310071884.5 discloses the catalyst system and its technique of a kind of industrial sulphur-containing exhaust gas desulfurization process, this is urged Change system includes polyalcohol, acidic catalyst and water, and reaction process uses low temperature aqueous phase reactions, while not containing H to two stocks2S And SO2Exhaust gas handled, total sulfur removal rate is improved to 99.95%.
CN201610841891.2 discloses a kind of preparation method of sulphur nanoparticulate dispersion, and this method is mainly in solution H is carried out in phase2S and SO2Redox reaction, the mixing of solution Xiang Weishui or Small molecule organic solvents soluble easily in water and water Solution, the Small molecule organic solvents being added are ethyl alcohol, methanol, dimethylformamide etc., in order to which the sulphur made is received Rice grain has better dispersion stabilization；40~80 DEG C of above-mentioned system reaction temperature, is in solution mutually during the reaction Stirring, so that H2S and SO2It sufficiently and is uniformly mixed in solution phase, the small and uniform sulphur nanometer of size can be made Grain dispersion liquid, the sulphur active material as secondary power supply technology (lithium-sulfur cell etc.).
CN201110075021.6 discloses a kind of containing H2The sulfur method of S mixed gas is 0 ~ 80 DEG C in reaction temperature, H will be contained2S and SO2Mixed gas is passed through the spray absorber or Spray column for being marked with tetramethyl guanidine hydroxy-acid salt composite desulfurizing agent Middle circulation, the two is reacted in the liquid phase generates sulphur.
Korean Institute of Science and Technology discloses a kind of while removing H in CN200580018462.52S and SO2Desulfurization Method, aqueous solution of the mixed gas with water or containing the first different-phase catalyst for desulfurization contact, to utilize SO2To aoxidize H2S, The treatment effeciency of tail gas containing 3 ~ 5% sulphur can be up to 99% or more.
Compagnie Francise des Petroles has applied a series of containing H2S and SO2The processing method and equipment of mixed gas, In CN200610058953.9 disclosed method, the temperature that mixed gas is in contact with the solvent containing catalyst system is 20 ~ 160 DEG C, catalyst system at least contains the functional group A being made of carboxylic acid functional at least one and has at least one functional group B Compound, functional group B have at least one nitrogen-atoms and under conditions of implementing the method at least one function Group A carries out acid-base class reaction；CN97120663.5, CN96196144.9 and CN97120546.9 are individually disclosed to containing H2S With SO2The processing method and equipment of mixed gas.
In above-mentioned disclosed patent, H2S and SO2Pressure, temperature and the pH value for reacting required in pure water are very severe It carves, reaction is both needed to that buffer solution or catalyst is added in organic solvent or aqueous solution, to keep organic solvent or aqueous solution is Acidity, acid stronger (pH value is lower) are more conducive to the progress of reaction, and device needs regular replenishment buffer solution or catalysis when running Agent is to keep reacting required acid condition, thus device operating cost increases；It is slow due to containing in resulting liquid phase sulphur iodine solution Solution or catalyst are rushed, the purity of sulfur product is unable to satisfy the market demand, thus needs mating sulphur refining plant to improve sulphur The purity of sulphur product.
Summary of the invention
It is harsh to solve hydrogen sulfide in the prior art and sulfur dioxide liquid-phase reaction condition, or need buffer solution, catalysis Agent, and caused by solid sulfur the problems such as product purity is low, purification is difficult, the present invention is quasi- to provide a kind of hydrogen sulfide and sulfur dioxide The technique of reaction desulfuration, hydrogen sulfide and sulfur dioxide react in liquid-phase system in the technique generates sulphur, and reaction condition is mild, tool There is higher desulfurization degree, the sulphur of purity is high can be obtained by simple solid-liquor separation.
To realize the above-mentioned technical purpose, the present invention provides the technique of a kind of hydrogen sulfide and sulfur dioxide reaction desulfuration, packets It including the following contents: hydrogen sulfide containing gas and the gas containing sulfur dioxide is passed through reactor, reactor is provided with reaction solution, The reaction solution includes water and at least one organic basic compound miscible with water, and the organic basic compound makes described PH value >=7.2 of solution；Hydrogen sulfide is reacted with sulfur dioxide generates sulphur, during the reaction takes out sulphur, and mend online Reaction solution is filled, or to after reaction separate the liquid in reactor admittedly, obtains sulphur.
In above-mentioned technique, as a further preference, the pH value of the reaction solution is 7.2 ~ 13.0 in reactor, excellent It is selected as 8.0 ~ 12.0.
In above-mentioned technique, as a further preference, the reaction solution presses its total weight, wherein organic basic The mass fraction for closing object is 0.1% ~ 30%, preferably 2% ~ 30%, more preferably 5% ~ 20%.
In above-mentioned technique, the organic basic compound is solubility >=0.1g/100g water chemical combination in water Object, preferably solubility >=1g/100g water.
In above-mentioned technique, it should be noted that the organic basic compound refers to that its acid-base property is organising for alkalinity Close object.Its selection is relatively broad, can be dissolved in water in principle, and has certain solubility in water, makes solution that the organic of alkalinity be presented Alkali compounds is the progress that can promote this desulphurization reaction, those energy and water can with the organic basic compound that arbitrary proportion dissolves each other To reach better effect.
In above-mentioned technique, as a further preference, the organic basic compound at least contains in its structural formula There is the compound of C1 ~ C10 of 1 nitrogen-atoms, the change of C1 ~ C10 further preferably in its structural formula containing 1 ~ 3 ammonia nitrogen Close object.
In above-mentioned technique, as a further preference, the organic basic compound in following compound extremely Few one kind: azanol, the fatty amines of C1 ~ C10, the alcamines of C1 ~ C10, the alicyclic ring amine of C1 ~ C10, C6 ~ C10 arylamine class, Pyridine, pyridine derivatives, imidazoles, imidazole derivative, pyrazine, Pyrazine derivative, pyrazoles or pyrazole derivatives.
Further, the pyridine derivatives, imidazole derivative, Pyrazine derivative or pyrazole derivatives are pyrrole The derivative that H in pyridine, imidazoles, pyrazine or pyrazoles is replaced by alkyl, amino, alkyl amino, hydroxyl or alkylol.The alkane The alkyl that alkyl in base, alkyl amino and alkylol is C1 ~ C3.
In above-mentioned technique, as further preferably, the fatty amines are the fatty amines of C1 ~ C6；The alcohol The arylamine class that alicyclic ring amine that alcamines that amine is C1 ~ C6, the alicyclic ring amine are C1 ~ C6, the arylamine class are C6 ~ C8.
As more specific embodiment, the organic basic compound is selected from azanol, trimethylamine, ethylenediamine, 1,2- third Diamines, 1,3- propane diamine, ethanol amine, diethanol amine, triethanolamine, diglycolamine, isopropanolamine, N methyldiethanol amine, N, N- dimethylethanolamine, N, N- diethyl ethylene diamine, benzene methanamine, O-phthalic amine, m-xylene diamine, p dimethylamine, tetrahydro Pyrroles, 1- methyl -3- pyrrolidinol, hexahydropyridine, morpholine, triethylenediamine, diethylenetriamines, piperazine, 2- methyl piperazine Piperazine, pyridine, 2- picoline, 3- picoline, 4- picoline, pyrazine, hydroxypyrazine, Aminopyrazine, methylpyrazine, imidazoles At least one of with pyrazoles.
It will be apparent to a skilled person that in the desulphurization reaction of hydrogen sulfide and sulfur dioxide, in liquid phase environment Under, the raising of pressure and temperature is conducive to the progress of reaction, and in previous research, the condition of desulphurization reaction occurs for the two liquid phase It is more harsh, it generally requires and improves reaction temperature and increase reaction pressure.But in the process of the invention, to hydrogen sulfide and dioxy The temperature and pressure for changing reaction of Salmon-Saxl desulfurization has no particular/special requirement, and from the point of view of saving the energy, control reactor is that room temperature is normal Pressure, the two can be easy to react.The reaction system new as one, the present invention still provide suitable reaction temperature and pressure Power: temperature is 0 ~ 90 DEG C, preferably 20 ~ 35 DEG C；Reaction pressure be 0.1 ~ 5MPa, preferably 0.1 ~ 1.5Mpa, more preferably often Pressure.
In above-mentioned technique, as a further preference, H in the reaction gas being passed through2S or SO2Volume fraction be respectively 0.1 ~ 100%, preferably 3 ~ 100%, more preferably 10 ~ 100%；The hydrogen sulfide containing gas is mainly derived from petroleum refining, coal Chemical industry, natural gas processing, fine chemistry industry, papermaking, pharmacy, chemical fertilizer, sewage treatment and geothermal power generation industrial tail gas pass through concentration Tail gas；Including but not limited to pure hydrogen sulfide, sour gas, Claus tail gases and natural gas purification tail gas etc..It is described Gas containing sulfur dioxide includes but is not limited to pure sulfur dioxide gas, S-Zorb device regenerated flue gas, Sulphuric acid tail gas, fire coal Boiler smoke, coal-fired plant flue gas, catalytic cracking catalyst regenerated flue gas, Furnace flue gas, coking flue gas and steel are burnt Tie flue gas etc., or the gas that the above flue gas is concentrated.
Further, the theoretical reaction ratio 2:1 of hydrogen sulfide and sulfur dioxide is preferably pressed in this process in reactor It is passed through according to 0.1:1 ~ 5:1 ratio, more preferably 1:1 ~ 3:1；Most preferably with the mixing of 2:1 ratio.If for the purpose of removing hydrogen sulfide, Then the gas containing sulfur dioxide is passed through by the reaction ratio amount of skipping over；If being omited for the purpose of scrubbing CO_2 by reaction ratio Excessively it is passed through hydrogen sulfide containing gas.
In above-mentioned technique, for H2S and SO2Be passed through sequence, the two can be passed through in reactor simultaneously, or be pre-mixed It is passed through in reactor together afterwards, or is first passed through one of reaction gas certain time, certain dissolution is reached in reaction solution After amount, then it is passed through another gas.It is wherein preferably first passed through a kind of reaction gas, is made in reactor after reaction solution pH < 7.0, then It is passed through another reaction gas, the two can more quickly and effectively react；With this corresponding, one is preferably provided in reactor A online pH detector；It is additionally provided with gas distributor at reactor bottom reactor inlet, disperses reaction gas preferably It is dissolved in reaction solution.
In above-mentioned technique, the tail gas after reaction is passed through in tail gas absorption tank, is lye or the present invention in tail gas absorption tank The reaction solution being related to, can be to unreacted H2S and SO2Equal Tail Gas realize absorbing and removing, then discharge to it.Make It after being absorbed with reaction solution of the invention, can also be recycled in reactor, make the H absorbed2S and SO2It is passed through in the external world Reaction gas drive lower further reaction, preferably handle pernicious gas.
In above-mentioned technique, it should be noted that the drusen generated in reactor in reaction process is in self gravity Deposited under effect to reactor bottom, sulphur slurries export continuously or intermittently online extraction from reactor bottom, and online to Reaction solution is supplemented in reactor；It, can be to which the slurries in reactor be taken together after reaction in the case where treating capacity is small Out；The sulphur slurries of taking-up can be obtained to the sulphur of high-purity by filtering, multiple washing and drying process；Wherein isolate Reaction solution, which can enter in tail gas absorption tank or reactor, to be recycled.
Compared with prior art, the present invention has the advantage that
(1) technique of hydrogen sulfide of the invention and sulfur dioxide reaction desulfuration uses the water containing organic basic compound for reaction Solution realizes H2S and SO2Desulphurization reaction under aqueous environment, and can realize reaction rapidly under normal temperature and pressure conditions；Have The addition of machine alkali compounds makes H2S and SO2Reaction time greatly shorten, both illustrate that rate of dissolution in water tends to phase Closely, to be easier to react.And on the other hand, with H2S and SO2Dissolution, the acid of reaction solution increase (pH therewith Value reduces), the addition bring alkalinity of organic basic compound has been neutralized, acidic environment is also beneficial to the progress of reaction, thus The rate that the two reaction generates sulphur greatly improves.
(2) in technique of the invention, H2S and SO2Can be reacted rapidly desulfurization at normal temperatures and pressures, reaction response Time is lower than 15 seconds, and required reaction condition is mild, the simple easy processing of equipment, low investment, safe operation, in the prior art The general requirement condition of desulphurization reaction under liquid-phase system is harsher, or needs catalyst, and for the reaction response time, generally At least more than a few minutes.
(3) in technique of the invention, the reaction solution used absorbs H2S and SO2It is not necessarily to buffer solution or catalyst afterwards It reacts and generates sulphur, reduce the operating cost of device, sulphur is free of buffer solution or catalyst in resulting slurries, only The sulphur of high-purity need to can be obtained, reduce the expense of sulphur purification, improve sulphur by simple solid-liquor separation without purification The purity of sulphur product.
(4) in technique of the invention, it can be used reaction solution of the invention as the absorbent of reaction end gas, can absorb Hydrogen sulfide and sulfur dioxide in reaction end gas make tail gas qualified discharge, and can recycle hydrogen sulfide and titanium dioxide in reaction end gas Sulphur further reacts, and increases the yield of sulphur and the processing capacity to exhaust gas.
(5) claus process after traditional and improvement is to H in unstripped gas2S content requires, and needs to reach 10% or more, It is lower for concentration to carry out entering Cross unit after concentrate processing；And reaction system of the invention is suitable for arbitrary proportion H2S and SO2Reaction, can cope with containing H2The sour gas of S and contain SO2Flue gas flow and the operating condition that changes greatly of composition.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
Fig. 1 is the process device figure of hydrogen sulfide and sulfur dioxide reaction desulfuration used in embodiment 1-9,12-29；
Fig. 2 is the process device figure of hydrogen sulfide and sulfur dioxide reaction desulfuration used in embodiment 10,11；
Wherein, 11. gas flowmeter I, 12. gas flowmeters II, 100. reactors, 101. gas distributors, 102.pH detection Instrument；200. separators, 300. tail gas absorption tanks, 400. tail gas absorbers.
Specific embodiment
Following non-limiting embodiments can with a person of ordinary skill in the art will more fully understand the present invention, but not with Any mode limits the present invention.
Embodiment 1
The technique for carrying out hydrogen sulfide and sulfur dioxide reaction desulfuration using device shown in FIG. 1 is as follows:
By pure SO2Gas is passed into 100 bottom of reactor through gas flowmeter I 11, and 100 bottom of reactor is provided with gas distribution Device 101, reactor 100 are provided with the aqueous solution of organic basic compound as reaction solution, SO2Gas is through gas distributor It is dissolved in reaction solution after 101, online pH detector 102 is provided on the wall of reactor 100, it is aobvious to pH detector 102 When being shown as 6.8, start to be passed through pure H into reactor 1002S gas is passed into reactor 100, instead after gas flowmeter II 12 The liquid in device 100 is answered to quickly become yellow, it is seen that the two immediate response generates sulphur；Product sulphur in reactor 100 with It is flowed out with part reaction solution from 100 bottom of reactor, separator 200 is squeezed by pump, separator 200 is by sulphur and reaction solution Separation, reaction solution can be passed through progress feed supplement in tail gas absorption tank 300 and recycle；Reaction end gas in reactor 100 passes through Top export enters tail gas absorption tank 300, and tail gas absorption tank 300 is provided with organic basic compound identical with reactor 100 Solution, the tail gas emptying after absorbing, the organic basic compound solution after absorbing tail gas is dissolved with the SO not reacted completely2With H2S, absorption return in reactor 100 that the reaction was continued after being substantially saturated, and supplement new organic basic compound solution thereto. Reaction temperature and pressure in reactor 100 are normal temperature and pressure.
Organic basic compound aqueous solution used in above-mentioned technique is benzene methanamine solution, mass fraction 30%, SO2 Gas flow is 300mL/min, H2S gas flow is 600mL/min.
It is to be installed set even running 2h after, the sulphur separating obtained to separator 200 is repeatedly washed, and title is dried Weight, according to MaterialBalance Computation, H2The conversion ratio of S is 93.5%.
Embodiment 2
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
In addition to organic basic compound solution is 20% benzene methanamine solution, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 94.1%.
Embodiment 3
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the isopropanolamine solution that organic basic compound solution is 20%, SO2Gas flow is 400mL/min, H2S gas Flow is outside 800mL/min, and other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 97.7%.
Embodiment 4
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
In addition to organic basic compound solution is 15% trimethylamine solution, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 97.2%.
Embodiment 5
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
The diglycolamine that organic basic compound solution used is 15%, H is first passed through into reactor2S gas, flow are 300mL/min when pH detector 102 is shown as 6.8, then is passed through SO thereto2Gas, flow 150mL/min, other Part is the same as embodiment 1.
According to MaterialBalance Computation, SO2Conversion ratio be 98.6%.
Embodiment 6
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
The pyridine that organic basic compound solution used is 5%, H is first passed through into reactor2S gas, flow 500mL/ Min when pH detector 102 is shown as 6.8, then is passed through SO thereto2Gas, flow 250mL/min, other conditions are the same as real Apply example 1.
According to MaterialBalance Computation, SO2Conversion ratio be 96.2%.
Embodiment 7
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the nafoxidine solution that organic basic compound solution is 2%, SO2Gas flow is 250mL/min, H2The stream of S gas Amount is outside 500mL/min, and other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 90.1%.
Embodiment 8
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
1- methyl -3- the pyrrolidinol that organic basic compound solution used is 0.5%, H is first passed through into reactor2S gas Body, flow 300mL/min when pH detector 102 is shown as 6.8, then are passed through SO thereto2Gas, flow 150mL/ Min, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, SO2Conversion ratio be 75.4%.
Embodiment 9
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except 1, the 3- propane diamine solution that organic basic compound solution is 20%, SO2Gas flow is 500mL/min, H2S gas Flow be 1000mL/min outside, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 99.2%.
Embodiment 10
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in Fig. 2:
Two kinds of reaction gas are first mixed to be passed through again in reactor 100 by Fig. 2 unlike Fig. 1 in induction part to react, with tail Aspiration tower 400 replaces the tail gas absorption tank 300 in Fig. 1, other settings and operation are the same as Fig. 1 in embodiment 1.
SO2Gas flow is 300mL/min, H2The flow of S gas is 600mL/min；By the device of Fig. 2, first by the two 100 bottom of reactor, the ethylenediamine solution that used organic basic compound solution is 10%, other behaviour are passed through after mixing again Make condition with embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 96.1%.
Embodiment 11
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in Fig. 2:
SO2Gas flow is 150mL/min, H2The flow of S gas is 300mL/min；Used organic basic compound is molten Terephthaldehyde's amine aqueous solution that liquid is 1%, other operating conditions are the same as embodiment 10.
According to MaterialBalance Computation, H2The conversion ratio of S is 71.8%.
Embodiment 12
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the triethylenediamine solution that organic basic compound solution is 20%, SO2Gas flow is 500mL/min, H2S gas The flow of body is outside 1000mL/min, and other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 99.3%.
Embodiment 13
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the piperazine solution that organic basic compound solution is 10%, SO2Gas flow is 350mL/min, H2The flow of S gas Outside for 700mL/min, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 97.9%.
Embodiment 14
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the pyrazine solution that organic basic compound solution is 3%, SO2Gas flow is 500mL/min, H2The flow of S gas is Outside 1000mL/min, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 95.5%.
Embodiment 15
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the hydroxypyrazine solution that organic basic compound solution is 5%, SO2Gas flow is 200mL/min, H2The stream of S gas Amount is outside 400mL/min, and other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 95.9%.
Embodiment 16
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the morpholine solution that organic basic compound solution is 25%, SO2Gas flow is 1000mL/min, H2The flow of S gas Outside for 2000mL/min, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 99.5%.
Embodiment 17
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the imidazole solution that organic basic compound solution is 10%, SO2Gas flow is 500mL/min, H2The flow of S gas Outside for 1000mL/min, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 98.6%.
Embodiment 18
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the pyrazoles solution that organic basic compound solution is 6%, SO2Gas flow is 500mL/min, H2The flow of S gas is Outside 1000mL/min, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 95.4%.
Embodiment 19
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the diethylenetriamines solution that organic basic compound solution is 5%, SO2Gas flow is 400mL/min, H2S gas Flow be 800mL/min outside, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 96.1%.
Embodiment 20
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the N methyldiethanol amine solution that organic basic compound solution is 10%, SO2Gas flow is 200mL/min, H2S The flow of gas is outside 400mL/min, and other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 99.2%.
Embodiment 21
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the N methyldiethanol amine solution that organic basic compound solution is 15%, SO2Gas uses S-Zorb regenerated flue gas (SO2Volume fraction is 4.5%) flow 500mL/min, H2S gas uses certain petroleum chemical enterprise's sour gas (dry gas, liquefied gas etc. The rich solution of desulfurizer regenerates generated sour gas, wherein H2S volume content be 55%), flow be 80mL/min outside, other Condition is the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 95.7%.
Embodiment 22
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the N that organic basic compound solution is 8%, N- dimethylethanolaminesolution solution, SO2Gas uses catalytic cracked regenerated cigarette Gas (SO2Volume fraction is 1.45%) flow 1000mL/min, H2S gas is using certain petroleum chemical enterprise's sour gas (submarine discharge acid Property gas, wherein H2S volume content is that 60%), flow is outside 50mL/min, and other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 92.1%.
Embodiment 23
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
In addition to organic basic compound solution is 20% triethanolamine solution, SO2Gas uses pure SO2, flow 300mL/ Min, H2S gas is using certain petroleum chemical enterprise's sour gas (sour gas after concentrate, wherein H295%) S volume content is that flow is 630mL/min, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 99.0%.
Embodiment 24
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the triethanolamine solution that organic basic compound solution is 12%, SO2Gas uses S-Zorb regenerated flue gas (SO2Volume Score is 4.5%) flow 1000mL/min, H2S gas is using certain the petroleum chemical enterprise's sour gas (desulfurization such as dry gas, liquefied gas dress The rich solution set regenerates generated sour gas, wherein H2S volume content is that 55%), flow is outside 160mL/min, and other conditions are same Embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 95.7%.
Embodiment 25
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the triethanolamine solution that organic basic compound solution is 6%, SO2Gas uses S-Zorb regenerated flue gas (SO2Volume Score is 4.5%) flow 1000mL/min, H2S gas is using certain the petroleum chemical enterprise's sour gas (desulfurization such as dry gas, liquefied gas dress The rich solution set regenerates generated sour gas, wherein H2S volume content is that 55%), flow is outside 160mL/min, and other conditions are same Embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 93.2%.
Embodiment 26
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except the 4- picoline solution that organic basic compound solution is 12%, SO2Gas uses fire coal boiler fume (SO2Volume Content is 0.5%) flow 5000mL/min, H2S gas using certain petroleum chemical enterprise's sour gas (sour gas after concentrate, Middle H2S volume content is that 95%), flow is outside 50mL/min, and other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 90.3%.
Embodiment 27
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except organic basic compound solution is the mixing amine aqueous solution containing 5% 2- picoline and 5% 1,2- propane diamine, SO2 Gas uses fire coal boiler fume (SO2Volume content is 0.5%) flow 3000mL/min, H2S gas uses certain petroleum chemical enterprise Sour gas (sour gas after concentrate, wherein H2S volume content is that 95%), flow is outside 30mL/min, and other conditions are the same as implementation Example 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 90.8%.
Embodiment 28
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except organic basic compound solution is the mixing amine aqueous solution containing 1% methylpyrazine and 9% N methyldiethanol amine, SO2Gas uses regeneration fume from catalytic cracking (SO2Volume fraction is 1.45%) flow 2000mL/min, H2S gas uses certain Petroleum chemical enterprise's sour gas (submarine discharge sour gas, wherein H2S volume content is that 60%), flow is other conditions outside 95mL/min With embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 92.7%.
Embodiment 29
The technique that hydrogen sulfide and sulfur dioxide reaction desulfuration are carried out using device shown in FIG. 1:
Except organic basic compound solution be containing 5% diethylenetriamines, 5% ethanol amine and 5% N, N- diethylaluminum ethoxide The mixing amine aqueous solution of amine, SO2Gas uses regeneration fume from catalytic cracking (SO2Volume fraction is 1.45%) flow 2000mL/ Min, H2S gas is using certain petroleum chemical enterprise's sour gas (submarine discharge sour gas, wherein H260%) S volume content is that flow is Outside 95mL/min, other conditions are the same as embodiment 1.
According to MaterialBalance Computation, H2The conversion ratio of S is 96.1%.

Claims (15)

1. the technique of a kind of hydrogen sulfide and sulfur dioxide reaction desulfuration, including the following contents: by hydrogen sulfide containing gas and containing two The gas of sulfur oxide is passed through reactor, and reactor is provided with reaction solution, and the reaction solution includes water and at least one and water The organic basic compound to dissolve each other, the organic basic compound make pH value >=7.2 of the solution；Hydrogen sulfide and sulfur dioxide Reaction generates sulphur, during the reaction takes out sulphur, and supplement reaction solution online, or to after reaction by reactor Interior liquid is separated admittedly, obtains sulphur.
2. technique according to claim 1, which is characterized in that in reactor the pH value of the reaction solution be 7.2 ~ 13.0, preferably 8.0 ~ 12.0.
3. technique according to claim 1, which is characterized in that the reaction solution presses its total weight, wherein organic base Property compound mass fraction be 0.1% ~ 30%, preferably 2% ~ 30%.
4. technique according to claim 1, which is characterized in that the organic basic compound is solubility in water The compound of >=0.1g/100g water, preferably solubility >=1g/100g water.
5. technique according to claim 1, which is characterized in that the organic basic compound in its structural formula at least The compound of C1 ~ C10 containing 1 nitrogen-atoms.
6. technique according to claim 5, which is characterized in that the organic basic compound contains in its structural formula The compound of C1 ~ C10 of 1 ~ 3 ammonia nitrogen.
7. technique according to claim 5, which is characterized in that the organic basic compound is in following compound It is at least one: azanol, the fatty amines of C1 ~ C10, the alcamines of C1 ~ C10, the alicyclic ring amine of C1 ~ C10, C6 ~ C10 arylamine Class, pyridine, pyridine derivatives, imidazoles, imidazole derivative, pyrazine, Pyrazine derivative, pyrazoles or pyrazole derivatives.
8. technique according to claim 7, which is characterized in that the pyridine derivatives, imidazole derivative, Pyrazine Derivative or pyrazole derivatives are the H in pyridine, imidazoles, pyrazine or pyrazoles by alkyl, amino, alkyl amino, hydroxyl or alkane The derivative that base alcohol replaces.
9. technique according to claim 8, which is characterized in that the alkyl in the alkyl, alkyl amino and alkylol is The alkyl of C1 ~ C3.
10. technique according to claim 7, which is characterized in that the fatty amines are the fatty amines of C1 ~ C6；It is described The arylamine that alicyclic ring amine that alcamines that alcamines is C1 ~ C6, the alicyclic ring amine are C1 ~ C6, the arylamine class are C6 ~ C8 Class.
11. technique according to claim 1, which is characterized in that the organic basic compound be selected from azanol, trimethylamine, Ethylenediamine, 1,2- propane diamine, 1,3- propane diamine, ethanol amine, diethanol amine, triethanolamine, diglycolamine, isopropanolamine, N- first Base diethanol amine, N, N- dimethylethanolamine, N are N- diethyl ethylene diamine, benzene methanamine, O-phthalic amine, m-xylene diamine, right Benzene dimethylamine, nafoxidine, 1- methyl -3- pyrrolidinol, hexahydropyridine, morpholine, triethylenediamine, diethylenetriamines, Piperazine, 2- methyl piperazine, pyridine, 2- picoline, 3- picoline, 4- picoline, pyrazine, hydroxypyrazine, Aminopyrazine, At least one of methylpyrazine, imidazoles and pyrazoles.
12. technique according to claim 1, which is characterized in that H in the reaction gas being passed through2S or SO2Volume fraction be 0.1 ~ 100%, preferably 3 ~ 100%.
13. technique according to claim 1, which is characterized in that the intake of reaction gas presses hydrogen sulfide and sulfur dioxide It is passed through for 0.1:1 ~ 5:1 ratio.
14. technique according to claim 1, which is characterized in that hydrogen sulfide containing gas and gas containing sulfur dioxide are same When be passed through, or be first passed through a kind of reaction gas and make in reactor after reaction solution pH < 7.0, then be passed through another reaction gas.
15. technique according to claim 1, which is characterized in that the tail gas after reaction is passed through in tail gas absorption tank, and tail gas is inhaled It is lye or the reaction solution in closed cans, the reaction solution is recycled to reactor, tail gas emptying after absorbing tail gas.
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