CN103787439A - Gas wetting purification desulfurizing solution zero-emission method - Google Patents
Gas wetting purification desulfurizing solution zero-emission method Download PDFInfo
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- CN103787439A CN103787439A CN201410064719.1A CN201410064719A CN103787439A CN 103787439 A CN103787439 A CN 103787439A CN 201410064719 A CN201410064719 A CN 201410064719A CN 103787439 A CN103787439 A CN 103787439A
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Abstract
The invention relates to a gas wetting purification desulfurizing solution zero-emission method, and belongs to the technical field of energy-saving and environment-friendly and comprehensive utilization of gas purification procedures. According to the technical scheme, the method comprises the following steps: installing a vacuum concentration tank, leading high-temperature desulfurizing solution discharged from a sulphur melter into a vacuum concentration tank, performing concentration and evaporation, and recycling residual heat; installing a hydraulic ejector used as a vacuumizing device on the vacuum concentration tank, adopting the desulfurizing solution as a spray liquid of the hydraulic ejector, installing a cooling crystallization device, recycling solid with more than 99% secondary salt content as side products, and recycling the liquid, obtained after the solid is separated, as a mother liquid into a desulfurizing solution, thus completely realizing the zero emission of the desulfurizing solution. By utilizing the characteristic that the sulphur melter is arranged in the existing gas purification desulfurization procedure, a steam cooling device is not needed to be separately arranged, energy consumption for cooling is not needed, the energy consumption can be greatly reduced and the running cost can be greatly lowered, the normal operation of the gas purification desulfurization technology can be ensured while the zero emission of desulfurizing solution can be realized, so that the method is energy-saving, environment-friendly, and synergistic.
Description
Technical field
The present invention relates to the method for a kind of gas wet purification doctor solution zero release, be particularly useful for the treatment process that the gas wet method catalytic desulfurizations such as coal gas, Sweet natural gas, coke(oven)gas purify doctor solution in production process, belong to the energy-saving and environmental protection of gas sweetening operation and comprehensive utilization technique field.
Background technology
The desulfurizing and purifying technique of gas is divided into dry method and the large class of wet method two, and wet desulphurization can remove the sulphur of high level, and simultaneously running cost is low and be widely adopted; The effective constituent that wet desulphurization doctor solution adopts mainly comprises ammoniacal liquor, soda ash etc., the H in effective constituent and the gas of doctor solution
2s carries out chemical reaction, H
2the reaction of the absorption reaction of S and reaction product oxidation regeneration hockets respectively and realizes removing continuously of sulphur in gas; Adopt soda ash as example take doctor solution effective constituent: to absorb H
2the chemical reaction of S is H
2s+Na
2cO
3=NaHS+NaHCO
3, the chemical reaction of oxidation regeneration is 2NaHS+2NaHCO
3+ O
2=2S ↓+2Na
2cO
3+ 2H
2o, the wet desulphurization in theory effective constituent of doctor solution is not lost, and does not also have other impurity to generate, but in actual production process, has by product to generate; Doctor solution effective constituent adopts soda ash, and secondary salt mainly contains three kinds: Na
2s
2o3, Na
2sO4, NaCNS; Doctor solution effective constituent adopts ammoniacal liquor, and secondary salt mainly comprises (NH
4)
2s
2o3, (NH
4)
2sO4, NH
4cNS; Adopt soda ash as example take doctor solution effective constituent, in the time that in doctor solution, secondary salt content is lower, Na
2s
2o
3≤ 100g/L, Na
2sO
4≤ 40g/L, NaSCN≤40g/L is less to gas desulfurization and purification technogenic influence, and outer row of doctor solution, recycles for a long time; When secondary salt content severe overweight in doctor solution is such as Na
2s
2o
3when>=200g/L is even higher, significantly decline of desulfuration efficiency, sweetening agent and supplementary product onsumption are significantly upper long, and gas purifying technique cannot normally carry out, and be forced to discharge unit doctor solution, supplement the new doctor solution of part and reduce secondary salt content, the discharge of doctor solution causes serious environmental pollution; Constantly riseing along with energy prices in recent years, the increasing raw material as producing coal gas and coking of high sulphur coal of high sulfur content gas extraction, low price, make the sulphur content in the gases such as coal gas, coke(oven)gas, Sweet natural gas more and more higher, especially on a large scale, atm number, H
2during the gas sweetening that S content is higher is produced, the generation of a large amount of secondary salts has had a strong impact on desulfuration efficiency, desulphurization cost obviously increases, and arranges steathily doctor solution and causes the phenomenon of environmental pollution to happen occasionally.
For above problem, someone has proposed to reduce the method for side reaction, as described in China Patent No. 200610166305.5, adds part of auxiliary to suppress the generation of side reaction in doctor solution, in the time that the sulphur content in gas is lower, there is certain effect, when the sulphur content in gas exceedes 2g/Nm
3when even higher, produce little effect; Someone has proposed doctor solution and has removed the method for secondary salt, as described in China Patent No. 200710014351.8, partial desulfurization liquid is drawn, obtain more than 90% secondary salt crystalline mixture through precipitation, decolouring, evaporation, after cooling, water after evaporative condenser is recovered in doctor solution, and it is that energy consumption and running cost are too high that this method exists subject matter: one is the effective constituent that contains partial desulfurization liquid in more than 90% secondary salt, comprises catalyzer etc., be removed with secondary salt, caused great waste; The 2nd, the water vapor condensation that doctor solution evaporates is that water will consume a large amount of heat-eliminating medium and power, and energy consumption is too high, and desulphurization cost will increase considerably; Somebody has proposed the method for doctor solution recovery secondary salt and recycle thereof as described in China Patent No. 201110097197.1, this method complex process, and operation easier is large, and running cost is high, and the auxiliary post that is not suitable as gas sweetening operation adopts.
Summary of the invention
The object of this invention is to provide the method for a kind of gas wet purification doctor solution zero release, vacuum concentration groove is set, do not need to set up water vapor refrigerating unit, do not need to consume cooling energy consumption, significantly reduce energy consumption and running cost, when realizing doctor solution zero release, guarantee normally carrying out of gas sweetening sulfur removal technology, energy-saving and environmental protection, synergy, solve the problems referred to above that exist in background technology.
The object of the present invention is achieved like this:
The method of a kind of gas wet purification doctor solution zero release, comprise following processing step: 1. vacuum concentration groove is set, adopt the high-temperature condensation water of sulfur melting kettle discharge as the thermal source of vacuum concentration groove, the high temperature desulfurizing liquid that sulfur melting kettle is discharged is introduced vacuum concentration groove, under low pressure, cold condition, make the evaporation of doctor solution partial concentration, recycle the high temperature desulfurizing liquid of sulfur melting kettle discharge and the waste heat of water of condensation;
vacuum concentration groove configuration hydraulic ejector, as vacuum extractor, adopts the atomizing of liquids of doctor solution as hydraulic ejector, and the water vapor of vacuum concentration groove evaporation is directly desulfurized liquid and absorbs, and does not need to arrange cool-down condensing device, does not need to consume cooling energy consumption;
equipment of crystallisation by cooling is set, doctor solution after concentrated is through cooling, Crystallization Separation, and solid is secondary salt, obtains more than 99% solid of secondary salt content and reclaims as byproduct, liquid after separate solid is that mother liquor is recovered in doctor solution, realizes the zero release of doctor solution completely.
The effect of described sulfur melting kettle is that the elemental sulfur in sulphur foam and doctor solution are separated, and the doctor solution temperature of discharge is 100-110 ℃, and the thermal source saturated vapour pressure that sulfur melting kettle adopts is 0.4-0.6MPa(a), the condensate temperature of discharge is 110-130 ℃; Controlling vacuum concentration groove pressure is 10-40KPa(a), vaporization temperature 60-80 ℃, hydraulic ejector adopts doctor solution as atomizing of liquids, recycle pump can be set separately, also can adopt the outlet of desulphurization system lean pump to separate a small part flow as atomizing of liquids.
Because active constituent content in doctor solution is lower, fall far short apart from the state of reaching capacity, and secondary salt content is relatively high, from state of saturation close to; For example: adopt soda ash as example take doctor solution effective constituent, doctor solution temperature is 40 ℃, Na in doctor solution under perfect condition
2cO
3content 5-10g/L, Na
2s
2o
3content≤100g/L; Na 40 ℃ time
2cO
3solubleness be 490g/L, Na
2s
2o
3solubleness be 776g/L; Na in doctor solution
2cO
3content keeps 10g/L constant, works as Na
2s
2o
3content 300g/L, in theory by concentrated the doctor solution under this state 49 times of Na
2cO
3ability crystallization, just has Na and concentrate 2.6 times
2s
2o
3crystallization; As Na in doctor solution
2s
2o
3when content is 150g/L, concentrated 5.17 times just have Na
2s
2o
3crystallization; Actual operation parameters is difference to some extent, discharge amount and the height of secondary salt content wherein of doctor solution according to sulfur melting kettle, control vacuum concentration doctor solution cycles of concentration 1-10 doubly, best 2-5 doubly, after dehydration separates, secondary salt content is more than 99% in the crystallization obtaining, and the mother liquor after fractional crystallization contains sweetening agent effective constituent, catalyzer, uncrystallized secondary salt etc. and is all recovered in doctor solution.
The present invention is applicable to all kinds of wet-method gas desulfurization systems and adopts, and is specially adapted to be provided with all kinds of wet-method gas desulfurization system applies of sulfur melting kettle.
The present invention is by arranging vacuum concentration groove, by the high temperature desulfurizing liquid of discharging after molten sulfur melting kettle sulphur, introduce vacuum concentration groove, adopt the high-temperature condensation water of sulfur melting kettle discharge as the thermal source of vacuum concentration groove, hydraulic ejector is set simultaneously, the device vacuumizing as vacuum concentration groove, hydraulic ejector adopts doctor solution as atomizing of liquids, the steam of vacuum concentration groove top outlet directly enters injector and is desulfurized liquid absorption, the liquid of vacuum concentration groove bottom after concentrated is through cooling, Crystallization Separation, crystallization is secondary salt, liquid after fractional crystallization is mother liquor, mother liquor is recovered in doctor solution, continuous or be interrupted cutting out partial secondary salt, effectively the secondary salt content in control doctor solution is within index, less energy-consumption, low cost realizes doctor solution zero release.
The doctor solution of the injected device of water vapor of vacuum concentration groove evaporation absorbs, and does not need to set up water vapor refrigerating unit, does not need to consume cooling energy consumption; Because the amount of this part water vapor is very little, account for the 0.1-1% of the total doctor solution internal circulating load of gas sweetening, very little on the temperature impact of doctor solution; Fully reclaim and utilize the high temperature desulfurizing liquid of sulfur melting kettle discharge and the waste heat of high-temperature condensation water, under low pressure, cold condition, by doctor solution part evaporation concentration, significantly reducing energy consumption and running cost.
The present invention utilizes gas desulfurization and purification operation to be provided with the feature of sulfur melter device, arrange vacuum concentrating apparatus by sulfur melting kettle discharge doctor solution in low pressure, part evaporation under low temperature, adopt doctor solution to absorb as the atomizing of liquids of vacuum extractor hydraulic ejector the water vapor evaporating, the doctor solution that sulfur melting kettle is discharged, and the waste heat of the water of condensation of discharging is all recycled as the energy, doctor solution after concentrated is cooling, crystallization is that secondary salt separates as byproduct and reclaims, mother liquor is recovered in doctor solution, less energy-consumption, low cost is separated the secondary salt in doctor solution, maintain secondary salt content in doctor solution within index, when realizing doctor solution zero release, guarantee normally carrying out of gas sweetening sulfur removal technology, energy-saving and environmental protection, synergy, solve the problems referred to above that exist in background technology.
Positively effect of the present invention is: utilize existing gas sweetening desulfurization process to be provided with the feature of sulfur melting kettle, set up vacuum concentrating apparatus, and configure hydraulic ejector as vacuum extractor, adopt the high-temperature condensation water of sulfur melting kettle discharge as the thermal source of vacuum concentrating apparatus, adopt the atomizing of liquids of doctor solution as hydraulic ejector, the high temperature desulfurizing liquid that sulfur melting kettle is discharged is introduced vacuum concentrating apparatus, at low temperature, under low pressure condition, carry out part evaporation concentration, the water vapor evaporating is absorbed by the injection desulfurization liquid of hydraulic ejector, water vapor has all been recovered in doctor solution, liquid after concentrated is through cooling, Crystallization Separation, solid secondary salt reclaims as byproduct, liquids recovery after separation secondary salt is in doctor solution, realize the zero release of doctor solution, compared with background technology, simple to operate, reliably, energy consumption is low, running cost is low.
Accompanying drawing explanation
Fig. 1 is that the embodiment of the present invention adopts the front process flow diagram of the present invention;
Fig. 2 is process flow diagram after embodiment of the present invention employing the present invention.
Embodiment
By the following examples, the invention will be further described:
With reference to accompanying drawing 1, background technology, employing coal is raw material, fixed bed atmospheric pressure gasification, the desulfurization at normal-pressure system of 200,000 tons of scales of annual output synthetic ammonia, doctor solution effective constituent is soda ash, phthalein mountain valley with clumps of trees and bamboo cobalt is catalyzer, the about 400m of doctor solution total volume
3, the about 1200m of desulphurization system doctor solution internal circulating load
3/ h, enters the about 20m of sulphur foam volume of sulfur melting kettle
3/ h, sulfur melting kettle thermal source is 0.5MPa(a) saturation steam, the about 2-2.5m of sulfur melting kettle outlet desulfurization liquid measure
3/ h, the about 3000-4000kg/ days of elemental sulfur output, the about 3-4t/h of steam consumption; Before adopting the present invention, 100-110 ℃ of doctor solution of sulfur melting kettle outlet has directly been recovered in doctor solution, the water of condensation of 110-130 ℃ of the sulfur melting kettle discharge normal pressure that reduces pressure, after discharge unit exhaust steam, being recovered to water treatment uses as soft water, when secondary salt content in doctor solution is lower, the not outer row of doctor solution, desulfuration efficiency is more than 95%, and ton ammonia soda ash consumes 3-3.5kg; Along with the raising of doctor solution secondary salt content, desulfuration efficiency progressively drops to below 90%, and the consumption of ton ammonia soda ash is analyzed Na in doctor solution more than bringing up to 5kg
2s
2o
3more than content has reached 200g/L, other secondary salt content also obviously raise, and are forced to regularly each discharge 30-100m
3doctor solution, the new doctor solution that supplements equal volume maintains production, and annual ton ammonia alkali consumption maintains 4.5-5kg, more than discharging every year doctor solution 300t, environment has been caused to serious pollution, and environmental protection pressure is huge.
Embodiment adopts the present invention, with reference to accompanying drawing 2, vacuum concentration evaporator is set, and configures hydrojet vacuum extractor, sulfur melting kettle outlet 100-110 ℃, about 2-2.5m
3/ h doctor solution enters vacuum concentration evaporator and carries out concentration and evaporation, the water of condensation of 110-130 ℃ of sulfur melting kettle discharge is as the thermal source of vacuum concentration evaporator, the cryogenic condensation water of 70-90 ℃ of discharge is recovered to water treatment and uses as soft water, in the time that the secondary salt content in doctor solution is 200g/L, cycles of concentration is doubly controlled by 4-5, and the liquid after evaporation concentration is 0.3-0.4m
3/ h, temperature 60-80 ℃, the amount that cooling, Crystallization Separation obtains secondary salt is 50-70kg/h, secondary salt reclaims as byproduct, the amount 0.2-0.3m of mother liquor
3/ h, be recovered in doctor solution, continuously-running of the present invention, also can intermitten service, in the time that secondary salt content is lower, take the way of intermitten service, annual separable go out the amount 200-300 ton of secondary salt, realize doctor solution zero release completely, secondary salt content in guaranteeing doctor solution zero release in effective control doctor solution is within index, the desulfuration efficiency that continues to remain higher and lower desulfurization alkaline consumption and supplementary product onsumption, adopt the present invention afterwards compared with not adopting the present invention, doctor solution is arranged outward and is reduced by 100%, desulfurization alkaline consumption and supplementary product onsumption reduce more than 10%, desulphurization cost reduces more than 10%, energy-conservation and environmental benefit is remarkable.
Claims (3)
1. the method for gas wet purification doctor solution zero release, it is characterized in that comprising following processing step: 1. vacuum concentration groove is set, adopt the high-temperature condensation water of sulfur melting kettle discharge as the thermal source of vacuum concentration groove, the high temperature desulfurizing liquid that sulfur melting kettle is discharged is introduced vacuum concentration groove, under low pressure, cold condition, make the evaporation of doctor solution partial concentration, recycle the high temperature desulfurizing liquid of sulfur melting kettle discharge and the waste heat of water of condensation;
vacuum concentration groove configuration hydraulic ejector, as vacuum extractor, adopts the atomizing of liquids of doctor solution as hydraulic ejector, and the water vapor of vacuum concentration groove evaporation is directly desulfurized liquid and absorbs, and does not need to arrange cool-down condensing device, does not need to consume cooling energy consumption;
equipment of crystallisation by cooling is set, doctor solution after concentrated is through cooling, Crystallization Separation, and solid is secondary salt, obtains more than 99% solid of secondary salt content and reclaims as byproduct, liquid after separate solid is that mother liquor is recovered in doctor solution, realizes the zero release of doctor solution completely.
2. the method for a kind of gas wet purification doctor solution according to claim 1 zero release, the effect that it is characterized in that described sulfur melting kettle is that the elemental sulfur in sulphur foam and doctor solution are separated, the doctor solution temperature of discharging is 100-110 ℃, the thermal source saturated vapour pressure that sulfur melting kettle adopts is 0.4-0.6MPa(a), the condensate temperature of discharge is 110-130 ℃.
3. the method for a kind of gas wet purification doctor solution according to claim 1 and 2 zero release, it is characterized in that controlling vacuum concentration groove pressure is 10-40KPa(a), vaporization temperature 60-80 ℃, hydraulic ejector adopts doctor solution as atomizing of liquids, and recycle pump is set separately; Or adopt the outlet of desulphurization system lean pump to separate a small part flow as atomizing of liquids.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106082137A (en) * | 2016-06-21 | 2016-11-09 | 山东铁雄冶金科技有限公司 | A kind of comprehensively utilize coking low-quality sulfur and the system of doctor solution secondary salt and technique |
| CN107352679A (en) * | 2017-07-11 | 2017-11-17 | 河南中鸿集团煤化有限公司 | A kind of doctor solution salt extraction technique and its device |
| CN110803731A (en) * | 2019-10-22 | 2020-02-18 | 中国石油化工集团有限公司 | Method and system for extracting secondary salt in high-sulfur-capacity complex iron desulfurization solution |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1262220A (en) * | 2000-01-31 | 2000-08-09 | 郑曙光 | Process and equipment for preparing sulfur from sulfur foam |
| CN101597522A (en) * | 2009-06-29 | 2009-12-09 | 朱春阳 | A kind of desulfuration processing method of coke oven gas and isolated plant thereof |
| CN102259894A (en) * | 2011-05-27 | 2011-11-30 | 山东美科动力有限公司 | Comprehensive recovery process of secondary salts from coking plant desulfurization waste liquid |
| CN102295379A (en) * | 2011-06-30 | 2011-12-28 | 首钢总公司 | Method for treating desulfurization waste liquid of wet oxidation method |
| CN102863111A (en) * | 2011-07-07 | 2013-01-09 | 河南殷都化工有限公司 | Novel ammonia water catalyzed coke-oven gas desulphurization recycling salt-extraction process |
| CN103058442A (en) * | 2013-01-25 | 2013-04-24 | 甘肃银光聚银化工有限公司 | Method for processing secondary salt in desulphurization waste liquid |
-
2014
- 2014-02-26 CN CN201410064719.1A patent/CN103787439B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1262220A (en) * | 2000-01-31 | 2000-08-09 | 郑曙光 | Process and equipment for preparing sulfur from sulfur foam |
| CN101597522A (en) * | 2009-06-29 | 2009-12-09 | 朱春阳 | A kind of desulfuration processing method of coke oven gas and isolated plant thereof |
| CN102259894A (en) * | 2011-05-27 | 2011-11-30 | 山东美科动力有限公司 | Comprehensive recovery process of secondary salts from coking plant desulfurization waste liquid |
| CN102295379A (en) * | 2011-06-30 | 2011-12-28 | 首钢总公司 | Method for treating desulfurization waste liquid of wet oxidation method |
| CN102863111A (en) * | 2011-07-07 | 2013-01-09 | 河南殷都化工有限公司 | Novel ammonia water catalyzed coke-oven gas desulphurization recycling salt-extraction process |
| CN103058442A (en) * | 2013-01-25 | 2013-04-24 | 甘肃银光聚银化工有限公司 | Method for processing secondary salt in desulphurization waste liquid |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106082137A (en) * | 2016-06-21 | 2016-11-09 | 山东铁雄冶金科技有限公司 | A kind of comprehensively utilize coking low-quality sulfur and the system of doctor solution secondary salt and technique |
| CN106082137B (en) * | 2016-06-21 | 2018-02-23 | 山东铁雄冶金科技有限公司 | A kind of system and technique for comprehensively utilizing coking low-quality sulfur and doctor solution secondary salt |
| CN107352679A (en) * | 2017-07-11 | 2017-11-17 | 河南中鸿集团煤化有限公司 | A kind of doctor solution salt extraction technique and its device |
| CN107352679B (en) * | 2017-07-11 | 2022-01-07 | 河南中鸿集团煤化有限公司 | Desulfurization liquid salt extraction process and device thereof |
| CN110803731A (en) * | 2019-10-22 | 2020-02-18 | 中国石油化工集团有限公司 | Method and system for extracting secondary salt in high-sulfur-capacity complex iron desulfurization solution |
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