CN104826465A - Multi-stage countercurrent absorption process and system for acidic gas - Google Patents
Multi-stage countercurrent absorption process and system for acidic gas Download PDFInfo
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- CN104826465A CN104826465A CN201410046324.9A CN201410046324A CN104826465A CN 104826465 A CN104826465 A CN 104826465A CN 201410046324 A CN201410046324 A CN 201410046324A CN 104826465 A CN104826465 A CN 104826465A
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Abstract
The invention provides a multi-stage countercurrent absorption process and system for acidic gas. The absorption process employs a gas-liquid two-phase countercurrent absorption reaction and uses a NaOH solution as an absorption liquid to treat acidic gas so as to produce NaHS. According to the process, a crystallizer and a separator are arranged in a primary reaction and a secondary reaction, and heat is taken out of a reactor; and through filling of the NaOH solution in stages, peak clipping of reaction heat is realized, and local crystallization caused by generation of heat spots is prevented. A combination of a Venturi reactor and a rotating packed bed reactor is used as a reaction apparatus which is flexible to operate and has high mass transfer efficiency. The acidic gas absorption process provided by the invention is simple and can achieve the dual objectives of purification of acidic gas and reclamation of pollutants; and the acidic gas absorption system has the advantages of small scale, low energy consumption and low proneness to obstruction.
Description
Technical field
The invention provides a kind of sour gas multi-stage countercurrent absorption technique method and system, belong to sour gas field of purification, to be particularly a kind ofly suitable for containing the purification of sulfohydrate sour gas and the processing method of pollutant resources and system.
Background technology
Sour gas mainly comes from the devices such as sewage stripping, desulphurization of recycle hydrogen, dry gas desulfurization, main containing H in sour gas
2s, CO
2.The sour gas of the small-sized refinery of current major part adopts the processing method of post combustion emission substantially.This method causes the waste of resource on the one hand, brings huge pressure on the other hand, affect the development space of enterprise to environmental protection.For protection of the environment and guarantee making full use of of resource, recycling is carried out to the sour gas of small-sized refinery imperative.
The process of big-and-middle-sized sour gas, mainly utilizes sour gas to prepare sulphur, and that relatively commonly uses at present has two kinds of technologies, and one is secondary Claus+ tail gas hydrogenation reduction+solvent absorption process technology; Another kind is the LO-CAT technology of gas technology Products Co., Ltd of Merichem company of U.S. exploitation.
Secondary Claus+ tail gas hydrogenation reduction+solvent absorption technical matters maturation, stable operation, product sulphur steady quality, but due to long flow path, investment large, Claus technique can only process the sour gas of high concentration, usually as the H in unstripped gas
2when S volume fraction is less than 20%, device just not easily operates.Therefore, Claus technique is suitable for the device producing more than sulphur 5000t per year.
LO-CAT technique adopts the iron catalyst of multicomponent chelate to make H
2s is converted into elementary sulfur, H
2the removal efficiency of S is more than 99.9%.LO-CAT technique can be applicable to acid tolerance and fluctuate comparatively greatly and H
2s content 0 ~ 100% various operating modes, raw material condition of compatibility is wide in range, adapt to sour gas fluctuation change actual conditions.And LO-CAT liquid redox treatment scheme does not use any poisonous chemicals, and can not produce any harmful exhaust gas by-products, environmentally safe catalyst constantly can regenerate in processing procedure.But due to LO-CAT have that operating cost is high, sulfur purity and color and luster be slightly worse than claus process; and the sulphur particle produced in process of production meeting blockage phenomenon; therefore, LO-CAT technique economy poor (relative to secondary Claus+ tail gas hydrogenation reduction+solvent absorption technology) in the following scale of annual output sulphur 5000t.
For small-sized refinery, because acid tolerance is relatively little, adopt secondary Claus+ tail gas hydrogenation reduction+solvent absorption technical matters to there is long flow path, complicated operation, investment greatly, scale and benefit are poor.And adopt LO-CAT technology also to exist once to invest comparatively large, catalyst and the problem such as patent royalties are higher.
Less for the total tolerance of small-sized sour gas, the new desulfurization process that investment is less can be adopted, by H
2s reclaims and prepares sulphite, first sour gas is carried out burning and generates SO
2, then send into absorption tower and carry out chemical absorbing generation sulfite solution, then solution and alkaline absorbent are reacted, prepare sulphite fluid product, or generate sulphite crystal, be prepared into sulphite solid product through operations such as separation, dryings.This device flow process is shorter, reaction is simple, operating flexibility is large, the impact of small-sized sour gas fluctuation on production process can be adapted to, solid or fluid product is produced by selecting different operations, select different absorbents can produce dissimilar sulphite, and realize tail gas qualified discharge by three sections of absorptions, realize the object of cleaning of off-gas.But it is serious to there is equipment corrosion in actual production process, the determination that maintenance cost is higher.
CN101143714A discloses a kind of method utilizing the acid gas to prepare sulfuric acid of high hydrocarbon-containing, acid hydrogen sulfide gas enters respectively in proportion in first, second sulfureted hydrogen burning stove and burns, from the first combustion furnace high-temperature furnace gas out, pass through burner-gas cooler, by Air flow to uniform temperature, then enter the second combustion furnace to continue to burn together with surplus air in furnace gas with the sulfide hydrogen sour gas supplemented, second combustion furnace high-temperature furnace gas out enters waste heat boiler heat accumulation, then enter purification section, conversion section, dry absorption section carry out conventional relieving haperacidity.This process can only produce 98% industrial sulphuric acid, can not the higher oleum of productive value, meanwhile, due to sulfuric acid transport, store and all acquire a certain degree of difficulty, therefore, the market demand stable near oil plant is the key factor limiting its development.
CN1836767A discloses a kind of processing method of oil-extraction plant acidic gas, utilizes sour gas as the fuel of cement plant shaft kiln, sour gas when kiln combustion, H wherein
2s composition and cement material generation chemical reaction and generate CaSO
4, other harmful components are also sintered and transform, and fundamentally solve a difficult problem for Acidic Gas Treating, simultaneously; sour gas, as a kind of gaseous fuel, makes cement plant energy-saving fuel, realizes the dual purpose of environmental protection and solution fuel; but this method has certain limitation, be not easy to promote.
CN101337661A mono-kind prepares in the method for NaHS, and the sour gas first adopting caustic soda and milk of lime to absorb containing hydrogen sulfide and carbon dioxide respectively generates intermediate liquid, then mixes in proportion, obtains the NaHS product of low-carbon (LC) acid group.The method does not require that sour gas is purer hydrogen sulfide gas, but flow process is longer, and automaticity is low.
Document " producing vulcanized sodium industrial technology with sodium hydroxide solution absorbing hydrogen sulphide " (give birth by Shangfang, " inorganic chemicals industry ", 44th volume the 2nd phase, in February, 2012) hydrogen sulfide sodium hydroxide solution absorbs and produces the production technology of vulcanized sodium by this technique, with 380 ~ 420g/L sodium hydroxide solution absorbing hydrogen sulphide in packed tower, control of reaction end point vulcanized sodium mass concentration is 330 ~ 350g/L, and hydrogen sulfide absorption rate reaches 95% ~ 98%.This technique not only can available protecting environment, and can be enterprise and create benefit.But this process products vulcanized sodium is apt to deteriorate, and not easily stores.
At present, for small-sized sour gas, need a kind of Acidic Gas Treating method considering the factors such as safety, environmental protection, economy.
Summary of the invention
For deficiency of the prior art, the invention provides a kind of sour gas multi-stage countercurrent absorption technique method and system, compared with prior art, sour gas multi-stage countercurrent absorption technique method and system of the present invention produces the NaHS product met the demands while realizing sour gas qualified discharge, realizes the double goal of sour gas purification and pollutant resources.
Sour gas absorption technique method of the present invention take NaOH solution as absorbing liquid, and process sour gas produces NaHS, comprises the steps:
(1) sour gas enters A reactor, and contact with the reaction solution of second reactor and react, reaction solution divides two-way, and the first via is discharged as product, and the second tunnel enters A reactor after Crystallization Separation;
(2) enter second reactor through step (1) reacted sour gas, to contact with the generation liquid of three reactor with NaOH solution and react; Reaction solution divides two-way, and the first via enters A reactor as absorbing liquid, and the second tunnel enters second reactor after Crystallization Separation;
(3) enter three reactor through step (2) reacted sour gas, generate liquid with fourth-order reaction device and contact and react, reaction solution divides two-way, and the first via enters second reactor as absorbing liquid, and the second tunnel loops back three reactor;
(4) enter fourth-order reaction device through step (3) reacted sour gas, react with NaOH solution, reacted sour gas discharge, reaction solution divides two-way, and the first via enters three reactor as absorbing liquid, and the second tunnel loops back fourth-order reaction device.
In present invention process method, in step (1), the volume flow ratio that the second road reaction solution and A reactor overall reaction generate liquid is 1/3 ~ 9/10, is preferably 5/6 ~ 8/9.
In present invention process method, in step (2), the volume flow ratio that the second road reaction solution and second reactor overall reaction generate liquid is 1/3 ~ 9/10, is preferably 5/6 ~ 8/9.
In present invention process method, in step (3), the volume flow ratio that the second road reaction solution and three reactor overall reaction generate liquid is 1/3 ~ 9/10, is preferably 5/6 ~ 8/9.
In present invention process method, in step (4), the volume flow ratio that the second road reaction solution and the overall reaction of fourth-order reaction device generate liquid is 1/3 ~ 9/10, is preferably 5/6 ~ 8/9.
In present invention process method, in the sour gas after step (4) process, hydrogen sulfide content is 5-30 mg/Nm
3.
In present invention process method, the sour gas after step (4) process discharges further after coalescer demist.
In present invention process method, the volume flow ratio of the NaOH solution addition of second reactor, fourth-order reaction device is 1:1 ~ 3:1, is preferably 3:2 ~ 2:1.
In present invention process method, the consumption of NaOH solution is design load, according to H in sour gas
2s, CO
2the fixed value that content is determined, according to the amount of sour gas, according to H in sour gas
2s and CO
2complete reaction calculates required NaOH solution amount, and design load is 80 ~ 99% of required NaOH solution consumption, is preferably 85 ~ 95%.
In present invention process method, the addition of NaOH solution is regulated by hydrogen sulfide content in the sour gas after step (4) process, regulate NaOH solution addition by control valve, ensure that in the sour gas after step (4) process, hydrogen sulfide content is 5-30mg/Nm
3, and at guarantee H
2when S qualified discharge, NaOH solution is inexcessive.
In present invention process method, described sour gas is hydrogen sulfide containing gas, can be various source containing H
2s sour gas, CO in described sour gas
2volume fraction be less than 7%, be preferably less than 5%.Described NaOH solution mass concentration is 20% ~ 60%, is preferably 32% ~ 38%.
In present invention process method, A reactor and second reactor reaction temperature are 70 DEG C ~ 100 DEG C, are preferably 80 DEG C ~ 95 DEG C.
In present invention process method, three reactor and fourth-order reaction device reaction temperature are 60 DEG C ~ 90 DEG C, are preferably 65 DEG C ~ 80 DEG C.
In present invention process method, described A reactor, second reactor, three reactor, fourth-order reaction device are one or more in bubbling column reactor, packed tower reactor, impact flow reactor, rotary drill reactor and venturi reactor.
In present invention process method, three reactor, fourth-order reaction device are preferably rotary drill reactor.
In present invention process method, A reactor, second reactor are preferably venturi reactor.
In present invention process method, described venturi reactor divides three sections from top to bottom, and epimere is liquid phase storage tank, and stage casing is straight tube reaction tube, and hypomere is gas-liquid separation cylinder; Described straight tube reaction tube is followed successively by feed zone, contraction section, trunnion section, expansion segment and discharging section from top to bottom; Feed zone top and liquid phase storage tank form sleeve structure, and discharging section bottom is connected with gas-liquid separation cylinder, and liquid phase storage tank is provided with gas phase entrance, and gas phase entry position is higher than end entrance on feed zone, and liquid phase storage tank sidewall is provided with circulation fluid entrance; The tube wall of straight tube reaction tube is provided with absorbing liquid entrance, and absorbing liquid entrance is positioned at trunnion top; Gas-liquid separation cylinder is provided with gaseous phase outlet and liquid-phase outlet.
In present invention process method, A reactor and second reactor adopt venturi reactor, and the reaction solution that described second tunnel loops back A reactor enters A reactor from circulation fluid entrance and absorbing liquid entrance respectively.The reaction solution entering A reactor from circulation fluid entrance is 1/6 ~ 1/2 with the reaction solution volume flow ratio entering A reactor from absorbing liquid entrance, is preferably 1/4 ~ 1/3.The reaction solution that second tunnel loops back second reactor enters A reactor from circulation fluid entrance and absorbing liquid entrance respectively.The reaction solution entering second reactor from circulation fluid entrance is 1/6 ~ 1/2 with the reaction solution volume flow ratio entering second reactor from absorbing liquid entrance, is preferably 1/4 ~ 1/3.
In present invention process method, described venturi reactor, teeth groove is offered in feed zone upper end, and tooth slot structure is the one in fan-shaped teeth groove, square teeth groove and triangle teeth groove, is preferably triangle tooth slot structure.Space width is 3mm ~ 20mm, preferred 5mm ~ 8mm; Bottom it, angle is 15 ~ 90 °, preferably 30 ~ 60 °.
In present invention process method, described venturi reactor, absorbing liquid entrance connects liquid phase distributor, and liquid phase distributor is arranged on straight tube reaction tube center line, sprays absorbing liquid from top to bottom, and liquid phase distributor can arrange 1 ~ 10, preferably 4 ~ 6.
In present invention process method, three reactor and fourth-order reaction device adopt rotary drill reactor, and the rotating speed of the revolving bed of rotary drill reactor is 50 ~ 5000 revs/min, are preferably 150 ~ 2000 revs/min.Reaction mass time of staying in reactor is 2 ~ 600 seconds, is preferably 10 ~ 100 seconds.
In present invention process method, control A reactor discharge liquid phase be NaHS solution, products pot detect by analysis qualified after, start to pump out device through product, realize continuous discharge.
A kind of sour gas absorption system of the present invention, described system comprises A reactor, second reactor, three reactor, fourth-order reaction device, one-level pans, secondary pans, three grades of pans, level Four pans, first degree crystalline device, secondary crystallizer, one-level knockout drum and the second-order separation tanks, wherein, A reactor, second reactor, three reactor and fourth-order reaction device arrange gas phase entrance, gaseous phase outlet, liquid phase entrance and liquid-phase outlet respectively; Sour gas suction line is connected with A reactor gas phase entrance, the gaseous phase outlet of A reactor is connected with the gas phase entrance of second reactor, the gaseous phase outlet of second reactor is connected with the gas phase entrance of three reactor, the gaseous phase outlet of three reactor is connected with the gas phase entrance of fourth-order reaction device, fourth-order reaction device gaseous phase outlet is connected with clean gas outlet pipeline, and clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear; Second reactor is connected with alkali liquor inlet pipeline respectively with the liquid phase entrance of fourth-order reaction device, and fourth-order reaction device liquid-phase outlet is divided into two-way after level Four pans, is connected respectively with three reactor liquid phase entrance and fourth-order reaction device liquid phase entrance; Three reactor liquid-phase outlet is connected with three reactor liquid phase entrance and second reactor liquid phase entrance respectively after three grades of pans; Second reactor liquid-phase outlet divides two-way, and the first via is connected with A reactor liquid phase entrance, and the second tunnel is connected with second reactor liquid phase entrance successively after secondary crystallizer, the second-order separation tank, secondary pans; A reactor liquid-phase outlet divides two-way, and the first via is connected with product discharge pipeline, and the second tunnel is connected with A reactor liquid phase entrance successively after first degree crystalline device, one-level knockout drum, one-level pans.
Sour gas absorption system of the present invention, described first degree crystalline device and secondary crystallizer arrange make-up cooling water entrance and circulating backwater outlet respectively.
Sour gas absorption system of the present invention, between fourth-order reaction device gaseous phase outlet and clean gas outlet pipeline, be provided with coalescer, described coalescer is cylindrical tube, and end socket comprises upper cover and low head, inside arranges cylindric screen cloth, prevents purified gas entrainment.
Sour gas absorption system of the present invention, described A reactor, second reactor, three reactor, fourth-order reaction device are gas-liquid mass transfer consersion unit, are specially one or more in bubbling column reactor, packed tower reactor, impact flow reactor, rotary drill reactor and venturi reactor.
Sour gas absorption system of the present invention, A reactor, second reactor are preferably venturi reactor, and three reactor, fourth-order reaction device are preferably rotary drill reactor.
The invention provides a kind of sour gas absorption system, described system comprises A reactor, second reactor, three reactor, fourth-order reaction device, one-level pans, secondary pans, three grades of pans, level Four pans, first degree crystalline device, secondary crystallizer, one-level knockout drum and the second-order separation tanks; Wherein, A reactor, second reactor are venturi reactor, and described venturi reactor divides three sections, and epimere is liquid phase storage tank, and stage casing is straight tube reaction tube, and hypomere is gas-liquid separation cylinder; Described straight tube reaction tube is followed successively by feed zone, contraction section, trunnion section, expansion segment and discharging section from top to bottom; Feed zone top and liquid phase storage tank form sleeve structure, and discharging section is connected with gas-liquid separation cylinder, and liquid phase storage tank is provided with gas phase entrance, and gas phase entry position is higher than end entrance on feed zone, and liquid phase storage tank sidewall is provided with circulation fluid entrance; The tube wall of straight tube reaction tube is provided with absorbing liquid entrance, and absorbing liquid entrance is positioned at trunnion top; Gas-liquid separation cylinder is provided with gaseous phase outlet and liquid-phase outlet; Three reactor and fourth-order reaction device arrange gas phase entrance, gaseous phase outlet, absorbing liquid entrance and liquid-phase outlet respectively; Sour gas suction line is connected with A reactor gas phase entrance, the gaseous phase outlet of A reactor is connected with the gas phase entrance of second reactor, the gaseous phase outlet of second reactor is connected with the gas phase entrance of three reactor, the gaseous phase outlet of three reactor is connected with the gas phase entrance of fourth-order reaction device, fourth-order reaction device gaseous phase outlet is connected with clean gas outlet pipeline, and clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear; Second reactor is connected with alkali liquor inlet pipeline respectively with the absorbing liquid entrance of fourth-order reaction device, and fourth-order reaction device liquid-phase outlet is divided into two-way after level Four pans, is connected respectively with three reactor absorbing liquid entrance and fourth-order reaction device absorbing liquid entrance; Three reactor liquid-phase outlet is connected with three reactor absorbing liquid entrance and second reactor absorbing liquid entrance respectively after three grades of pans; Second reactor liquid-phase outlet divides two-way, and the first via is connected with A reactor absorbing liquid inlet, and the second tunnel is connected with second reactor absorbing liquid entrance and circulation fluid entrance respectively successively after secondary crystallizer, the second-order separation tank, secondary pans; A reactor liquid-phase outlet divides two-way, and the first via is connected with product discharge pipeline, and the second tunnel is connected with A reactor absorbing liquid entrance and circulation fluid entrance respectively successively after first degree crystalline device, one-level knockout drum, one-level pans.
Sour gas absorption system of the present invention, described first degree crystalline device and secondary crystallizer arrange make-up cooling water entrance and circulating backwater outlet respectively.
Sour gas absorption system of the present invention, described venturi reactor, feed zone upper end is for offering teeth groove, and tooth slot structure is the one in fan-shaped teeth groove, square teeth groove and triangle teeth groove, is preferably triangle tooth slot structure.Space width is 3mm ~ 20mm, preferred 5mm ~ 8mm; Bottom it, angle is 15 ~ 90 °, preferably 30 ~ 60 °.
Sour gas absorption system of the present invention, described venturi reactor, absorbing liquid entrance connects liquid phase distributor, and liquid phase distributor is arranged on straight tube reaction tube center line, sprays absorbing liquid from top to bottom, and liquid phase distributor can arrange 1 ~ 10, preferably 4 ~ 6.Absorbing liquid entrance is arranged on the straight tube reaction tube outer wall on contraction section top, is preferably arranged between liquid phase storage tank bottom and contraction section.
Sour gas absorption system of the present invention, the gas-liquid separation cylinder of described venturi reactor arranges heat-obtaining facility, and control temperature is 85 DEG C ~ 120 DEG C, is preferably 90 DEG C ~ 95 DEG C, prevents intermediate product crystallization.
Compared with prior art, sour gas absorption technique method of the present invention and device tool have the following advantages:
1, sour gas absorption technique method of the present invention, adopt level Four gas-liquid two-phase counter-current absorption course of reaction, the self-loopa being provided with reaction solution absorbs operation again, improve reaction depth, material is fully contacted with sour gas, guarantee that NaHS liquid-phase product meets national product quality standard, Na in product NaHS
2the content of S is less than 4%; Circulated by reaction mass, alkali lye is fully contacted with sour gas, makes H in purified gas
2s content is lower than 30 mg/Nm
3, guarantee that the sour gas after processing realizes the target of qualified discharge.
2, sour gas absorption technique method of the present invention, NaOH solution is added by classification, respectively to second reactor, fourth-order reaction device filling NaOH solution, regulate response intensity at different levels, peak clipping process is carried out to reaction heat, ensures temperature of reactor at different levels in the reasonable scope, prevent heat spot, cause local-crystalized, cause reaction terminating.
3, sour gas absorption technique method of the present invention, by arranging first degree crystalline device, one-level knockout drum, secondary crystallizer, the second-order separation tank, reaction solution enters temperature-controllable low temperature crystallization device, reactant liquor is ejected into the cryogenic tube bundle outer surface of crystallizer through spraying into mist shape, ordered crystalline is realized at tube bank outer surface, annular scraper is set outside cryogenic tube bundle, outer for tube bank crystal is scraped in solution, and enter knockout drum fast, realize liquid, Gu be separated, realize crystal to remove, reduce the solid holdup that intermediate reaction generates liquid, improve object product yield and purity, and take out part reaction heat, reduce the concentration raising of evaporating and causing, prevent crystallization.
4, adopt venturi reactor of the present invention as A reactor and second reactor, reaction solution enters reactor reservoir by the circulation fluid entrance of venturi reactor, when circulation fluid position is higher than feed zone entrance, the reaction solution of circulation forms overflow, whole wall of reactor distributes with wall stream form, uniform liquid film is formed at reactor wall, take liquid film as division board, not only prevent crystal from separating out adhesive reaction device inwall, simultaneously, take liquid film as heat-absorbing medium, take out reaction heat, effectively prevent reaction solution excessive vaporization.
5, sour gas absorption plant of the present invention adopts high-gravity rotating bed as gas-liquid reactor, can realize the target improving mass transfer and reaction efficiency, rotary drill reactor is efficient mass transfer equipment, ensures that reaction is carried out fast, reduce the generation of side reaction, reduce impurity content in product.Meanwhile, because rotary drill reactor mass-transfer efficiency is hundreds of times of common tower reactor mass-transfer efficiency, reactor scale reduces greatly.And by CO in sour gas
2when reacting with NaOH, generate nano level Na
2cO
3crystalline solid, thus Na during the conveying of anti-fluid
2cO
3crystalline solid blocking pipe.Material, on the bed assembly inwall of high-speed rotation, forms hard hit, realizes strengthening mixing; Material, when flowing through bed, is constantly cut into drop, brin and liquid film by bed, the Surface Renewal greatly achieving high-viscosity material with mix, eliminate concentration difference, generate nano level Na
2cO
3crystalline solid.
6, sour gas absorption technique of the present invention and device are particularly useful for processing small-sized sour gas, and compared with prior art, equipment scale is little, energy consumption is low, and operating cost is few, generates the NaHS product that may be used for the industries such as printing and dyeing, papermaking, be convenient to transport, and have certain market value.
Accompanying drawing explanation
Fig. 1 is a kind of sour gas absorption technique method of the present invention and device schematic diagram.
Fig. 2 is the second sour gas absorption technique method of the present invention and device schematic diagram.
Fig. 3 is venturi reactor schematic diagram in the second sour gas absorption technique method of the present invention and device.
Detailed description of the invention
Sour gas counter-current absorption process of the present invention and device take NaOH solution as absorbing liquid, and process oil-extraction plant acidic gas produces NaHS product, adopt level Four gas-liquid two-phase counter-current absorption course of reaction.
As shown in Figure 1, the first sour gas absorption system of the present invention, described system comprises A reactor 1, second reactor 2, three reactor 3, fourth-order reaction device 4, first degree crystalline device 5, one-level knockout drum 6, one-level pans 7, secondary crystallizer 8, the second-order separation tank 9, secondary pans 10, three grades of pans 11, level Four pans 12, wherein, A reactor 1, second reactor 2, three reactor 3, fourth-order reaction device 4 arranges gas phase entrance respectively, gaseous phase outlet, liquid phase entrance and liquid-phase outlet, sour gas suction line 26 is connected with the gas phase entrance of A reactor, and the gaseous phase outlet of A reactor is connected with the gas phase entrance of second reactor, the gaseous phase outlet of second reactor is connected with the gas phase entrance of three reactor, the gaseous phase outlet of three reactor is connected with fourth-order reaction device gas phase entrance, and the gaseous phase outlet of fourth-order reaction device is connected with clean gas outlet pipeline 27, clean gas outlet pipeline 27 is provided with hydrogen sulfide content checkout gear 29, and alkali liquor inlet pipeline 13 is by pipeline 15, pipeline 14 is connected with the liquid phase entrance of secondary pans and fourth-order reaction device respectively, fourth-order reaction device liquid-phase outlet is divided into two-way after level Four pans 12, one tunnel 18 is connected with fourth-order reaction device liquid phase entrance, one tunnel 19 is connected with three reactor liquid phase entrance, three reactor liquid-phase outlet is point two-way after three grades of pans 11, one tunnel 20 is connected with three reactor liquid phase entrance, and another road 21 is connected with second reactor liquid phase entrance, second reactor liquid-phase outlet divides two-way, and the first via 22 is connected with A reactor liquid phase entrance, and the second tunnel 23 is connected with second reactor liquid phase entrance successively after secondary crystallizer 8, the second-order separation tank 9, secondary pans 10, A reactor liquid-phase outlet divides two-way, the first via 24 is connected with product discharge pipeline, second tunnel 25 is connected with A reactor liquid phase entrance successively after first degree crystalline device 5, one-level knockout drum 6, one-level pans 7, and described first degree crystalline device and secondary crystallizer are respectively arranged with make-up cooling water 16 and circulating backwater 17.
Shown in Fig. 1, sour gas multi-stage countercurrent absorption technique method of the present invention, first sour gas from sour gas suction line 26 enters A reactor 1, with the generation liquid haptoreaction from second reactor, reaction solution is divided into two-way, the first via is discharged as product, second tunnel enters first degree crystalline device, under the effect of make-up cooling water, crystallisation by cooling, then enter one-level knockout drum and carry out solid-liquor separation, be separated the liquid obtained and enter one-level pans, then circulation enters A reactor, sour gas after A reactor process enters second reactor 2, with from the generation liquid of three reactor and alkali lye NaOH haptoreaction, reaction solution is divided into two-way, the first via 22 enters A reactor as absorbing liquid through A reactor liquid phase entrance, second tunnel generates liquid and enters secondary crystallizer, under the effect of make-up cooling water, crystallisation by cooling, then enter one-level knockout drum and carry out solid-liquor separation, being separated the solid major part obtained is Na
2cO
3crystallization, may be used for sewage treatment plant after taking-up regulates PH to use, be separated the liquid obtained and enter secondary pans, second reactor is entered through pump, enter three reactor through the reacted sour gas of second reactor, generate liquid react with fourth-order reaction device, reacted generation liquid enters three grades of pans, then the first via 21 enters second reactor as absorbing liquid, and the second tunnel 20 loops back three reactor, fourth-order reaction device is entered through the reacted sour gas of three reactor, react with NaOH solution, reacted sour gas passes through clean gas outlet pipeline 27 qualified discharge after coalescer 28 further demist, reacted generation liquid divides two-way after entering level Four pans, the first via 19 enters three reactor as absorbing liquid, second tunnel 18 loops back fourth-order reaction device, and described first degree crystalline device and secondary crystallizer are respectively arranged with make-up cooling water 16 and circulating backwater 17.
As shown in Figure 2, sour gas absorption system shown in the second embodiment of the present invention, described system comprises A reactor 1, second reactor 2, three reactor 3, fourth-order reaction device 4, one-level pans 7, secondary pans 10, three grades of pans 11, level Four pans 12, first degree crystalline device 5, secondary crystallizer 8, one-level knockout drum 6 and the second-order separation tanks 9; Wherein, A reactor, second reactor adopt venturi reactor, and described venturi reactor divides three sections from top to bottom, and epimere is liquid phase storage tank 34, and stage casing is straight tube reaction tube 30, and hypomere is gas-liquid separation cylinder 41; Described straight tube reaction tube is followed successively by feed zone 33, contraction section 37, trunnion section 38, expansion segment 39 and discharging section 40 from top to bottom; Feed zone top and liquid phase storage tank form sleeve structure, and discharging section 40 is connected with gas-liquid separation cylinder 41, and liquid phase storage tank is provided with gas phase entrance 31, and gas phase entry position is higher than end entrance on feed zone, and liquid phase storage tank sidewall is provided with circulation fluid entrance 32; The tube wall of straight tube reaction tube is provided with absorbing liquid entrance 35, and absorbing liquid entrance is positioned at trunnion top; Gas-liquid separation cylinder is provided with gaseous phase outlet 42 and liquid-phase outlet 43; Three reactor and fourth-order reaction device arrange gas phase entrance, gaseous phase outlet, absorbing liquid entrance and liquid-phase outlet respectively; Sour gas suction line 26 is connected with A reactor gas phase entrance, the gaseous phase outlet of A reactor is connected with the gas phase entrance of second reactor, the gaseous phase outlet of second reactor is connected with the gas phase entrance of three reactor, the gaseous phase outlet of three reactor is connected with the gas phase entrance of fourth-order reaction device, fourth-order reaction device gaseous phase outlet is connected with clean gas outlet pipeline 27, and clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear 29; Alkali liquor inlet pipeline 13 is connected with the liquid phase entrance of secondary pans and fourth-order reaction device respectively by pipeline 15, pipeline 14, fourth-order reaction device liquid-phase outlet is divided into two-way after level Four pans, one tunnel 19 is connected with three reactor absorbing liquid entrance, and another road 18 is connected with fourth-order reaction device absorbing liquid entrance; Three reactor liquid-phase outlet is point two-way after three grades of pans, and a road 20 is connected with three reactor absorbing liquid entrance, and a road 21 is connected with second reactor absorbing liquid entrance; Second reactor liquid-phase outlet divides two-way, the first via 22 is connected with A reactor absorbing liquid entrance, and the second tunnel 23 enters second reactor through second reactor absorbing liquid entrance and circulation fluid entrance respectively successively after secondary crystallizer 8, the second-order separation tank 9, secondary pans 10; A reactor liquid-phase outlet divides two-way, the first via 24 is connected with product discharge pipeline, second tunnel 25 enters A reactor through A reactor absorbing liquid entrance and circulation fluid entrance respectively successively after first degree crystalline device 5, one-level knockout drum 6, one-level pans 7, and described first degree crystalline device and secondary crystallizer are respectively arranged with make-up cooling water 16 and circulating backwater 17.
As shown in Figure 2, sour gas multi-stage countercurrent absorption technique method of the present invention, first sour gas from sour gas pipeline 26 enters A reactor 1, with the generation liquid haptoreaction from second reactor, reaction solution is divided into two-way, the first via is discharged as product, second tunnel enters first degree crystalline device, under the effect of make-up cooling water, crystallisation by cooling, then enter one-level knockout drum and carry out solid-liquor separation, be separated the liquid obtained and enter one-level pans, A reactor is entered respectively by A reactor absorbing liquid entrance and circulation fluid entrance, the first order reaction generation liquid entering A reactor through circulation fluid entrance forms downflow weir in A reactor, whole A reactor wall distributes with wall stream form, uniform liquid film is formed at reactor wall, take liquid film as division board, not only prevent crystal from separating out adhesive reaction device inwall, simultaneously, take liquid film as heat-absorbing medium, take out reaction heat, effectively prevent Na
2s solution excessive vaporization.Sour gas after A reactor process enters second reactor 2, with from the generation liquid of three reactor and alkali lye NaOH haptoreaction, reaction solution is divided into two-way, the first via enters A reactor as absorbing liquid through A reactor absorbing liquid entrance, second tunnel generates liquid and enters secondary crystallizer, under the effect of make-up cooling water, and crystallisation by cooling, then enter one-level knockout drum and carry out solid-liquor separation, being separated the solid major part obtained is Na
2cO
3crystallization, may be used for sewage treatment plant after taking-up regulates PH to use, be separated the liquid obtained and enter secondary pans, second reactor is entered respectively by second reactor absorbing liquid entrance and circulation fluid entrance, the second order reaction generation liquid entering second reactor through circulation fluid entrance forms downflow weir in second reactor, whole second reactor wall distributes with wall stream form, uniform liquid film is formed at reactor wall, take liquid film as division board, not only prevent crystal from separating out adhesive reaction device inwall, simultaneously, take liquid film as heat-absorbing medium, take out reaction heat, effectively prevent Na
2s solution excessive vaporization.Enter three reactor through the reacted sour gas of second reactor, generate liquid react with fourth-order reaction device, reacted generation liquid enters three grades of pans, and then a road enters second reactor as absorbing liquid, and the second tunnel loops back three reactor; Fourth-order reaction device is entered through the reacted sour gas of three reactor, react with NaOH solution, reacted sour gas after coalescer 28 demist through clean gas outlet pipeline 27 qualified discharge, reacted generation liquid divides two-way after entering level Four pans, the first via enters three reactor as absorbing liquid, and the second tunnel loops back fourth-order reaction device.
Sour gas multi-stage countercurrent absorption technique method of the present invention comprises following Four processes:
(1) course of reaction in A reactor
In A reactor, key reaction is as follows: undressed sour gas and second order reaction generate liquid and (mainly consist of Na
2s and NaHS, part Na
2cO
3, NaHCO
3mixed solution, at H
2when S is excessive, second order reaction generates the Na in liquid
2s and H
2s reacts, and generates NaHS and part NaHCO
3solution.Reaction solution enters temperature-controllable low temperature first degree crystalline device, and reactant liquor is ejected into cryogenic tube bundle outer surface through spraying into mist shape, realizes NaHCO at tube bank outer surface
3ordered crystalline, arranges annular scraper outside cryogenic tube bundle, scraped in solution by outer for tube bank crystal, and enter one-level knockout drum fast, realize liquid, be admittedly separated NaHCO
3, realize crystal and remove, reduce the solid holdup that intermediate reaction generates liquid, improve object product yield and purity, and take out part reaction heat, minimizing is evaporated the concentration caused and is improved, prevents crystallization.NaHS solution after realizing being separated divides two-way, and the first via is discharged through pipeline as product; Second tunnel enters first degree crystalline device, under the cooling effect of recirculated water, carries out ordered crystalline, then enters one-level knockout drum and carries out Separation of Solid and Liquid, is separated the liquid obtained and enters one-level pans.
(2) course of reaction in second reactor
In second reactor, key reaction is as follows: gas phase is " the weary gas " of first order reaction gas phase, wherein H
2s concentration is still higher, does not reach discharge standard; Second order reaction liquid phase is the mixed solution that alkali lye and third-order reaction generate liquid, at H
2when S is excessive, Na
2s and NaOH mixed liquor and H
2s reacts, and generates Na
2s and NaHS mixed liquor.Owing to carrying CO secretly in sour gas
2component, CO
2react with NaOH and generate Na
2cO
3, NaHCO
3.Reaction solution Na
2s, NaHS and part Na
2cO
3, NaHCO
3mixed liquor, reaction solution divides two-way, the first via enters A reactor as absorbing liquid, second tunnel enters secondary crystallizer, by the mode of the indirect heat-obtaining of recirculated water, generation liquid is cooled to 85 DEG C ~ 95 DEG C, reactant liquor is ejected into cryogenic tube bundle outer surface through spraying into mist shape, realizes Na at tube bank outer surface
2cO
3, NaHCO
3ordered crystalline, arranges annular scraper outside cryogenic tube bundle, scraped in solution by outer for tube bank crystal, and enter one-level knockout drum fast, realizes liquid, solid separation, isolates most of Na
2cO
3, NaHCO
3, realize crystal and remove, reduce intermediate reaction and generate the solid holdup of liquid, improve object product yield and purity, and take out part reaction heat, control the reaction temperature of second reactor, prevent from generating liquid and cross the concentration that thermal evaporation causes and improve, prevent crystallization.Liquid phase in knockout drum flows into pans by three grades of absorbing liquid transport pump to the second reactors, circulates.Second order reaction generates the Na in liquid
2cO
3, NaHCO
3crystallization reduce solid holdup in liquid phase, reduce production flow line and block the device that affects caused and normally produce.
(3) course of reaction in three reactor
In three reactor, key reaction is as follows: third-order reaction gas phase is " the weary gas " of second level reaction gas phase, wherein H
2s concentration reduces greatly, but still does not realize qualified discharge requirement.Third-order reaction generates liquid (most of NaOH and a small amount of Na with fourth-order reaction
2s mixed liquor) be absorbing liquid, at H
2when S is little over amount, NaOH and Na
2s mixed liquor and H
2s reacts, and generates Na
2s and NaHS, reaction solution divides two-way, and the first via enters second reactor as absorbing liquid, and the second tunnel generates liquid and enters in three reactor through pans, circulates, and the degree of depth realizing absorbing liquid absorbs and circulation heat-obtaining.
(4) course of reaction in fourth-order reaction device
In fourth-order reaction device, key reaction is as follows: fourth-order reaction gas phase is " the weary gas " of third level reaction gas phase, wherein H
2s concentration is extremely low, substantially reaches emission request.Fourth-order reaction is absorbing liquid with NaOH solution, at H
2when S is a small amount of, NaOH and H
2s reacts, and generates a small amount of Na
2s.
Below in conjunction with embodiment, the present invention is further described, but therefore do not limit the scope of the invention.
Embodiment 1
Adopt process as shown in Figure 1 and system, with sour gas and NaOH solution for raw material, react.CO in sour gas
2volume fraction is 7%, H
2s volume fraction is 92%, and hydro carbons volume fraction is 1%.NaOH solution mass concentration is 38%.
In embodiment 1, A reactor and second reactor adopt venturi reactor, three reactor and fourth-order reaction device adopt rotary drill reactor, and described venturi reactor and rotary drill reactor can be the general venturi reactor in this area and rotary drill reactor.
In embodiment 1, looping back the volume flow ratio that the second road reaction solution of A reactor and A reactor overall reaction generate liquid is 5:6.Looping back the volume flow ratio that the second road reaction solution of second reactor and second reactor overall reaction generate liquid is 5:6.Looping back the volume flow ratio that the second road reaction solution of three reactor and three reactor overall reaction generate liquid is 5:6.Looping back the volume flow ratio that the second road reaction solution of fourth-order reaction device and the overall reaction of fourth-order reaction device generate liquid is 5:6.
In embodiment 1, the alkali lye addition volume flow ratio of second reactor, fourth-order reaction device is 2:1.
In one-level venturi reactor and secondary venturi reactor, reaction temperature is the reaction temperature of 80 DEG C of three grades of rotary drill reactors and level Four rotary drill reactor is 75 DEG C.The rotating speed of the revolving bed of three grades of rotary drill reactors and level Four rotary drill reactor is 1500 revs/min.Three grades of rotary drill reactors and level Four rotary drill reactor reaction mass time of staying in reactor are 10 seconds, and reaction result is in table 1.
Embodiment 2
Adopt process as shown in Figure 2 and system, in embodiment 2, A reactor and second reactor adopt the venturi reactor shown in Fig. 3, and three reactor and fourth-order reaction device adopt rotary drill reactor.
In embodiment 2, looping back through A reactor absorbing liquid entrance the volume flow ratio that the reaction solution of A reactor and A reactor overall reaction generate liquid is 5:8.Looping back through A reactor circulation fluid entrance the volume flow ratio that the reaction solution of A reactor and A reactor overall reaction generate liquid is 5:24.
Looping back through second reactor absorbing liquid entrance the volume flow ratio that the reaction solution of second reactor and second reactor overall reaction generate liquid is 5:8.Looping back through second reactor circulation fluid entrance the volume flow ratio that the reaction solution of second reactor and second reactor overall reaction generate liquid is 5:24.
Looping back the volume flow ratio that the second road reaction solution of three reactor and three reactor overall reaction generate liquid is 5:6.Looping back the volume flow ratio that the second road reaction solution of fourth-order reaction device and the overall reaction of fourth-order reaction device generate liquid is 5:6.
In embodiment 2, the volume flow ratio of the alkali lye addition of second reactor, fourth-order reaction device is 2:1.
In one-level venturi reactor and secondary venturi reactor, reaction temperature is 80 DEG C.The reaction temperature of three grades of rotary drill reactors and level Four rotary drill reactor is 75 DEG C.The rotating speed of the revolving bed of three grades of rotary drill reactors and level Four rotary drill reactor is 1500 revs/min.Three grades of rotary drill reactors and level Four rotary drill reactor reaction mass time of staying in reactor are 10 seconds, and reaction result is in table 1.
Comparative example 1
Identical with embodiment 1, difference is that alkali lye is only annotated from fourth stage reactor.
Table 1 embodiment and comparative example reaction result
Claims (35)
1. a sour gas multi-stage countercurrent absorption technique method take NaOH solution as absorbing liquid, and process sour gas produces NaHS, comprises the steps:
(1) sour gas enters A reactor, and contact with the reaction solution of second reactor and react, reaction solution divides two-way, and the first via is discharged as product, and the second tunnel enters A reactor after Crystallization Separation;
(2) enter second reactor through step (1) reacted sour gas, to contact with the generation liquid of three reactor with NaOH solution and react; Reaction solution divides two-way, and the first via enters A reactor as absorbing liquid, and the second tunnel enters second reactor after Crystallization Separation;
(3) enter three reactor through step (2) reacted sour gas, generate liquid with fourth-order reaction device and contact and react, reaction solution divides two-way, and the first via enters second reactor as absorbing liquid, and the second tunnel loops back three reactor;
(4) enter fourth-order reaction device through step (3) reacted sour gas, react with NaOH solution, reacted sour gas discharge, reaction solution divides two-way, and the first via enters three reactor as absorbing liquid, and the second tunnel loops back fourth-order reaction device.
2. according to process according to claim 1, it is characterized in that: in step (1), looping back the volume flow ratio that the second road reaction solution of A reactor and A reactor overall reaction generate liquid is 1/3 ~ 9/10, is preferably 5/6 ~ 8/9.
3. according to process according to claim 1, it is characterized in that: in step (2), looping back the volume flow ratio that the second road reaction solution of second reactor and second reactor overall reaction generate liquid is 1/3 ~ 9/10, is preferably 5/6 ~ 8/9.
4. according to process according to claim 1, it is characterized in that: in step (3), looping back the volume flow ratio that the second road reaction solution of three reactor and three reactor overall reaction generate liquid is 1/3 ~ 9/10, is preferably 5/6 ~ 8/9.
5. according to process according to claim 1, it is characterized in that: in step (4), looping back the volume flow ratio that the second road reaction solution of fourth-order reaction device and the overall reaction of fourth-order reaction device generate liquid is 1/3 ~ 9/10, is preferably 5/6 ~ 8/9.
6. according to process according to claim 1, it is characterized in that: the volume flow ratio of the NaOH solution addition of second reactor, fourth-order reaction device is 1:1 ~ 3:1, be preferably 3:2 ~ 2:1.
7. according to process according to claim 1, it is characterized in that: the addition of NaOH solution is regulated by hydrogen sulfide content in the sour gas after step (4) process, regulate NaOH solution addition by control valve, ensure that in the sour gas after step (4) process, hydrogen sulfide content is 5-30 mg/Nm
3, and at guarantee H
2when S qualified discharge, NaOH solution is inexcessive.
8. according to process according to claim 1, it is characterized in that: the sour gas after step (4) process discharges further after coalescer demist.
9. according to process according to claim 1, it is characterized in that: in the sour gas after step (4) process, hydrogen sulfide content is 5-30 mg/Nm
3.
10. according to process according to claim 1, it is characterized in that: the reaction temperature of A reactor and second reactor is 70 DEG C ~ 100 DEG C, be preferably 80 DEG C ~ 95 DEG C.
11., according to process according to claim 1, is characterized in that: in three reactor and fourth-order reaction device, reaction temperature is 60 DEG C ~ 90 DEG C, are preferably 65 DEG C ~ 80 DEG C.
12. according to process according to claim 1, it is characterized in that: A reactor, second reactor, three reactor, fourth-order reaction device are gas-liquid mass transfer consersion unit, be specially one or more in bubbling column reactor, packed tower reactor, impact flow reactor, rotary drill reactor and venturi reactor.
13., according to process according to claim 1, is characterized in that: three reactor, fourth-order reaction device are rotary drill reactor.
14. according to process according to claim 13, it is characterized in that: three reactor and fourth-order reaction device adopt rotary drill reactor, the rotating speed of the revolving bed of three grades of rotary drill reactors and level Four rotary drill reactor is 50 ~ 5000 revs/min, is preferably 150 ~ 2000 revs/min.
15. according to process according to claim 13, it is characterized in that: three reactor and fourth-order reaction device adopt rotary drill reactor, reaction mass time of staying in three grades of rotary drill reactors and level Four rotary drill reactor is 2 ~ 600 seconds, is preferably 10 ~ 100 seconds.
16., according to process according to claim 1, is characterized in that: A reactor, second reactor are venturi reactor.
17., according to process according to claim 16, is characterized in that: described venturi reactor divides three sections from top to bottom, and epimere is liquid phase storage tank, and stage casing is straight tube reaction tube, and hypomere is gas-liquid separation cylinder; Described straight tube reaction tube is followed successively by feed zone, contraction section, trunnion section, expansion segment and discharging section from top to bottom; Feed zone top and liquid phase storage tank form sleeve structure, and discharging section bottom is connected with gas-liquid separation cylinder, and liquid phase storage tank is provided with gas phase entrance, and gas phase entry position is higher than end entrance on feed zone, and liquid phase storage tank sidewall is provided with circulation fluid entrance; The tube wall of straight tube reaction tube is provided with absorbing liquid entrance, and absorbing liquid entrance is positioned at trunnion top; Gas-liquid separation cylinder is provided with gaseous phase outlet and liquid-phase outlet.
18., according to process according to claim 17, is characterized in that: the reaction solution of the second road A reactor enters A reactor from circulation fluid entrance and absorbing liquid entrance respectively after Crystallization Separation.
19. according to process according to claim 18, it is characterized in that: the reaction solution entering A reactor from circulation fluid entrance is 1/6 ~ 1/2 with the reaction solution volume flow ratio entering A reactor from absorbing liquid entrance, is preferably 1/4 ~ 1/3.
20., according to process according to claim 17, is characterized in that: the reaction solution of the second road second reactor enters A reactor from circulation fluid entrance and absorbing liquid entrance respectively after Crystallization Separation.
21. according to process according to claim 20, it is characterized in that: the reaction solution entering second reactor from circulation fluid entrance is 1/6 ~ 1/2 with the reaction solution volume flow ratio entering second reactor from absorbing liquid entrance, is preferably 1/4 ~ 1/3.
22. according to process according to claim 17, it is characterized in that: described venturi reactor, teeth groove is offered in feed zone upper end, and tooth slot structure is the one in fan-shaped teeth groove, square teeth groove and triangle teeth groove, is preferably triangle tooth slot structure.
23., according to process according to claim 17, is characterized in that: described venturi reactor, and absorbing liquid entrance connects liquid phase distributor, liquid phase distributor is arranged on straight tube reaction tube center line, spray absorbing liquid from top to bottom, liquid phase distributor arranges 1 ~ 10, preferably 4 ~ 6.
24., according to process according to claim 1, is characterized in that: described sour gas is the hydrogen sulfide containing gas in various source, CO in sour gas
2volume fraction be less than 7%.
25., according to process according to claim 1, is characterized in that: described NaOH solution mass concentration is 20% ~ 60%, are preferably 32% ~ 38%.
The sour gas absorption system of the sour gas multi-stage countercurrent absorption technique method in 26. employing claims 1 to 25 described in arbitrary claim, it is characterized in that: described system comprises A reactor, second reactor, three reactor, fourth-order reaction device, one-level pans, secondary pans, three grades of pans, level Four pans, first degree crystalline device, secondary crystallizer, one-level knockout drum and the second-order separation tank, wherein, A reactor, second reactor, three reactor and fourth-order reaction device arrange gas phase entrance respectively, gaseous phase outlet, liquid phase entrance and liquid-phase outlet, sour gas suction line is connected with A reactor gas phase entrance, the gaseous phase outlet of A reactor is connected with the gas phase entrance of second reactor, the gaseous phase outlet of second reactor is connected with the gas phase entrance of three reactor, the gaseous phase outlet of three reactor is connected with the gas phase entrance of fourth-order reaction device, fourth-order reaction device gaseous phase outlet is connected with clean gas outlet pipeline, and clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear, second reactor is connected with alkali liquor inlet pipeline respectively with the liquid phase entrance of fourth-order reaction device, and fourth-order reaction device liquid-phase outlet is divided into two-way after level Four pans, is connected respectively with three reactor liquid phase entrance and fourth-order reaction device liquid phase entrance, three reactor liquid-phase outlet is connected with three reactor liquid phase entrance and second reactor liquid phase entrance respectively after three grades of pans, second reactor liquid-phase outlet divides two-way, and the first via is connected with A reactor liquid phase entrance, and the second tunnel is connected with second reactor liquid phase entrance successively after secondary crystallizer, the second-order separation tank, secondary pans, A reactor liquid-phase outlet divides two-way, and the first via is connected with product discharge pipeline, and the second tunnel is connected with A reactor liquid phase entrance successively after first degree crystalline device, one-level knockout drum, one-level pans.
27., according to system according to claim 1, is characterized in that: described first degree crystalline device and secondary crystallizer arrange make-up cooling water entrance and circulating backwater outlet respectively.
28. according to system according to claim 26, it is characterized in that: be provided with coalescer between fourth-order reaction device gaseous phase outlet and clean gas outlet pipeline, described coalescer is cylindrical tube, and end socket comprises upper cover and low head, and inside arranges cylindric screen cloth.
29. according to system according to claim 26, it is characterized in that: described A reactor, second reactor, three reactor, fourth-order reaction device are gas-liquid mass transfer consersion unit, be specially the one in bubbling column reactor, packed tower reactor, impact flow reactor, rotary drill reactor and venturi reactor.
30., according to system according to claim 26, is characterized in that: described A reactor, second reactor are venturi reactor, and three reactor, fourth-order reaction device are rotary drill reactor.
The sour gas utilization system of the sour gas comprehensive utilization process method in 31. employing claims 1 to 25 described in arbitrary claim, is characterized in that: described system comprises A reactor, second reactor, three reactor, fourth-order reaction device, one-level pans, secondary pans, three grades of pans, level Four pans, first degree crystalline device, secondary crystallizer, one-level knockout drum and the second-order separation tanks; Wherein, A reactor, second reactor are venturi reactor, and described venturi reactor divides three sections, and epimere is liquid phase storage tank, and stage casing is straight tube reaction tube, and hypomere is gas-liquid separation cylinder; Described straight tube reaction tube is followed successively by feed zone, contraction section, trunnion section, expansion segment and discharging section from top to bottom; Feed zone top and liquid phase storage tank form sleeve structure, and discharging section is connected with gas-liquid separation cylinder, and liquid phase storage tank is provided with gas phase entrance, and gas phase entry position is higher than end entrance on feed zone, and liquid phase storage tank sidewall is provided with circulation fluid entrance; The tube wall of straight tube reaction tube is provided with absorbing liquid entrance, and absorbing liquid entrance is positioned at trunnion top; Gas-liquid separation cylinder is provided with gaseous phase outlet and liquid-phase outlet; Three reactor and fourth-order reaction device arrange gas phase entrance, gaseous phase outlet, absorbing liquid entrance and liquid-phase outlet respectively; Sour gas suction line is connected with A reactor gas phase entrance, the gaseous phase outlet of A reactor is connected with the gas phase entrance of second reactor, the gaseous phase outlet of second reactor is connected with the gas phase entrance of three reactor, the gaseous phase outlet of three reactor is connected with the gas phase entrance of fourth-order reaction device, fourth-order reaction device gaseous phase outlet is connected with clean gas outlet pipeline, and clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear; Second reactor is connected with alkali liquor inlet pipeline respectively with the absorbing liquid entrance of fourth-order reaction device, and fourth-order reaction device liquid-phase outlet is divided into two-way after level Four pans, is connected respectively with three reactor absorbing liquid entrance and fourth-order reaction device absorbing liquid entrance; Three reactor liquid-phase outlet is connected with three reactor absorbing liquid entrance and second reactor absorbing liquid entrance respectively after three grades of pans; Second reactor liquid-phase outlet divides two-way, the first via is connected with A reactor absorbing liquid entrance, and the second tunnel is connected with second reactor absorbing liquid entrance and second reactor circulation fluid entrance respectively successively after secondary crystallizer, the second-order separation tank, secondary pans; A reactor liquid-phase outlet divides two-way, and the first via is connected with product discharge pipeline, and the second tunnel is connected with A reactor absorbing liquid entrance and A reactor circulation fluid entrance respectively successively after first degree crystalline device, one-level knockout drum, one-level pans.
32., according to system according to claim 31, is characterized in that: described first degree crystalline device and secondary crystallizer arrange make-up cooling water entrance and circulating backwater outlet respectively.
33., according to system according to claim 31, is characterized in that: described venturi reactor, and feed zone upper end is for offering teeth groove, and tooth slot structure is the one in fan-shaped teeth groove, square teeth groove and triangle teeth groove, are preferably triangle tooth slot structure.
34., according to system according to claim 31, is characterized in that: described venturi reactor, and absorbing liquid entrance connects liquid phase distributor, liquid phase distributor is arranged on straight tube reaction tube center line, spray absorbing liquid from top to bottom, liquid phase distributor can arrange 1 ~ 10, preferably 4 ~ 6.
35., according to system according to claim 31, is characterized in that: absorbing liquid entrance is arranged on the straight tube reaction tube outer wall on contraction section top, is preferably arranged between liquid phase storage tank bottom and contraction section.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105268305A (en) * | 2015-11-23 | 2016-01-27 | 金川集团股份有限公司 | Device and method for multistage cyclic absorption and desulfurization of active ore pulp |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4814104A (en) * | 1987-02-05 | 1989-03-21 | Uop | Tertiary alkanolamine absorbent containing an ethyleneamine promoter and its method of use |
| JP2005200456A (en) * | 2004-01-13 | 2005-07-28 | Sumitomo Chemical Co Ltd | Method of removing hydrogen sulfide |
| CN101092576A (en) * | 2006-06-23 | 2007-12-26 | 中国石油化工股份有限公司 | Method for removing acid gases in cracked gas |
| CN201746324U (en) * | 2010-06-21 | 2011-02-16 | 淄博高汇化工有限公司 | Device for reclaiming sodium sulfhydrate |
| CN102351153A (en) * | 2011-07-04 | 2012-02-15 | 山东雅美科技有限公司 | Method for producing sodium bisulfide products by viscose fiber industrial waste gas |
| CN102408100A (en) * | 2011-08-02 | 2012-04-11 | 山东雅美科技有限公司 | 22% sodium hydrosulfide product with low content of miscellaneous salt produced by utilizing viscose waste gas |
| CN202876623U (en) * | 2012-11-09 | 2013-04-17 | 沈阳广达化工有限公司 | Continuous absorption tower system of hydrogen sulfide in process of sulphide isobutene production |
-
2014
- 2014-02-10 CN CN201410046324.9A patent/CN104826465B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4814104A (en) * | 1987-02-05 | 1989-03-21 | Uop | Tertiary alkanolamine absorbent containing an ethyleneamine promoter and its method of use |
| JP2005200456A (en) * | 2004-01-13 | 2005-07-28 | Sumitomo Chemical Co Ltd | Method of removing hydrogen sulfide |
| CN101092576A (en) * | 2006-06-23 | 2007-12-26 | 中国石油化工股份有限公司 | Method for removing acid gases in cracked gas |
| CN201746324U (en) * | 2010-06-21 | 2011-02-16 | 淄博高汇化工有限公司 | Device for reclaiming sodium sulfhydrate |
| CN102351153A (en) * | 2011-07-04 | 2012-02-15 | 山东雅美科技有限公司 | Method for producing sodium bisulfide products by viscose fiber industrial waste gas |
| CN102408100A (en) * | 2011-08-02 | 2012-04-11 | 山东雅美科技有限公司 | 22% sodium hydrosulfide product with low content of miscellaneous salt produced by utilizing viscose waste gas |
| CN202876623U (en) * | 2012-11-09 | 2013-04-17 | 沈阳广达化工有限公司 | Continuous absorption tower system of hydrogen sulfide in process of sulphide isobutene production |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105268305A (en) * | 2015-11-23 | 2016-01-27 | 金川集团股份有限公司 | Device and method for multistage cyclic absorption and desulfurization of active ore pulp |
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