CN104826464A - Novel acidic gas treating process and apparatus - Google Patents
Novel acidic gas treating process and apparatus Download PDFInfo
- Publication number
- CN104826464A CN104826464A CN201410046323.4A CN201410046323A CN104826464A CN 104826464 A CN104826464 A CN 104826464A CN 201410046323 A CN201410046323 A CN 201410046323A CN 104826464 A CN104826464 A CN 104826464A
- Authority
- CN
- China
- Prior art keywords
- reactor
- liquid
- entrance
- gas
- phase
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a novel acidic gas treating process and apparatus. The acidic gas treating 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 primary liquid reaction product and a secondary liquid reaction product are cyclically used, the secondary liquid reaction product is used a tertiary reaction absorption liquid, and an MDEA solution is used as a fourth-stage reaction absorption liquid; thus, the purpose of replacement of CO2 with H2S is achieved, the generation amounts of Na2CO3 and NaHCO3 in a liquid phase product are reduced, precipitation of crystals is prevented, and long cycle operation of the apparatus is guaranteed. The acidic gas treating process provided by the invention is simple and can achieve the dual objectives of purification of acidic gas and reclamation of pollutants.
Description
Technical field
The invention provides a kind of Acidic Gas Treating technique and device, 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 device.
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 Acidic Gas Treating process and device, compared with prior art, Acidic Gas Treating process of the present invention and device produce the NaHS product met the demands while realizing sour gas qualified discharge, realize the double goal of sour gas purification and pollutant resources.
Acidic Gas Treating technique 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 loops back A reactor;
(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 tertiary road, and the first via enters A reactor as absorbing liquid, and the second tunnel loops back second reactor, and the 3rd tunnel enters three reactor as absorbing liquid;
(3) enter three reactor through step (2) reacted sour gas, generate liquid with the 3rd road second reactor and contact and react, reaction solution divides two-way, and the first via enters second reactor, and the second tunnel loops back three reactor;
(4) enter fourth-order reaction device through step (3) reacted sour gas, with methyl diethanolamine (MDEA) solution reaction, reacted sour gas discharge, reaction solution regeneration Posterior circle uses.
In present invention process, 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.
In present invention process, 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 1/2 ~ 8/9.
In present invention process, in step (2), entering as absorbing liquid the volume flow ratio that the 3rd road reaction solution of three reactor and second reactor overall reaction generate liquid is 1/6 ~ 1/2, is preferably 1/5 ~ 1/4.
In present invention process, 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 1/5 ~ 1/4.
In present invention process, in step (4), the liquid-gas ratio of MDEA solution and sour gas is 8L/m
3~ 15L/m
3between, be preferably 10L/m
3~ 12L/m
3.The mass concentration of MDEA solution is 20% ~ 50%, is preferably 30% ~ 40%.
In present invention process, 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, the addition of NaOH solution is regulated by hydrogen sulfide content in the sour gas after step (4) process, regulates NaOH solution addition by control valve, ensures 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, the sour gas after step (4) process discharges further after coalescer demist.In sour gas after step (4) process, hydrogen sulfide content is 5-30 mg/Nm
3.
In present invention process, the reaction temperature of A reactor and second reactor is 70 DEG C ~ 100 DEG C, is preferably 80 DEG C ~ 95 DEG C.
In present invention process, in three reactor and fourth-order reaction device, reaction temperature is 60 DEG C ~ 90 DEG C, is preferably 65 DEG C ~ 80 DEG C.
In present invention process, 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.
In present invention process, three reactor, fourth-order reaction device are rotary drill reactor.
In present invention process, three reactor and fourth-order reaction device adopt rotary drill reactor, and 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, are preferably 150 ~ 2000 revs/min.
In present invention process, three reactor and fourth-order reaction device adopt rotary drill reactor, and reaction mass time of staying in three grades of rotary drill reactors and level Four rotary drill reactor is 2 ~ 600 seconds, are preferably 10 ~ 100 seconds.
In present invention process, A reactor, second reactor are venturi reactor.
In present invention process, 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, the reaction solution that the second tunnel loops back A reactor enters A reactor from circulation fluid entrance and absorbing liquid entrance respectively.
In present invention process, 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.
In present invention process, the reaction solution that the second tunnel loops back second reactor enters A reactor from circulation fluid entrance and absorbing liquid entrance respectively.
In present invention process, 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, 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.
In present invention process, 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, 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, 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 Acidic Gas Treating device of the present invention, described device comprises A reactor, second reactor, three reactor, fourth-order reaction device, three grades of pans, level Four pans, 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, clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear, the liquid phase entrance of second reactor is connected with alkali liquor inlet pipeline, and the liquid phase entrance of fourth-order reaction device is connected with MDEA solution inlet pipeline, 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 is connected with A reactor liquid phase entrance, second reactor liquid phase entrance and three reactor liquid phase entrance respectively, A reactor liquid-phase outlet is connected with A reactor liquid phase entrance and product discharge pipeline respectively.
Acidic Gas Treating device of the present invention, is provided with coalescer between fourth-order reaction device gaseous phase outlet and clean gas outlet pipeline, and described coalescer is cylindrical tube, and end socket comprises upper cover and low head, and inside arranges cylindric screen cloth.
Acidic Gas Treating device of the present invention, described A reactor, second reactor, three reactor, fourth-order reaction device are gas-liquid mass transfer consersion unit, are specially the one in bubbling column reactor, packed tower reactor, impact flow reactor, rotary drill reactor and venturi reactor.
Acidic Gas Treating device of the present invention, described A reactor, second reactor are venturi reactor, and three reactor, fourth-order reaction device are rotary drill reactor.
Another kind of Acidic Gas Treating device of the present invention, described device comprises A reactor, second reactor, three reactor, fourth-order reaction device, three grades of pans, level Four pans, wherein, A reactor, second reactor are venturi reactor, described venturi reactor divides three sections, 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, clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear; The absorbing liquid entrance of second reactor is connected with alkali liquor inlet pipeline respectively, and fourth-order reaction device absorbing liquid entrance is connected with MDEA solution inlet pipeline; 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 is connected with A reactor absorbing liquid entrance, second reactor absorbing liquid entrance, second reactor circulation fluid entrance respectively and three reactor absorbing liquid entrance connects; A reactor liquid-phase outlet is connected with A reactor circulation fluid entrance, A reactor absorbing liquid entrance and product discharge pipeline respectively.
Acidic Gas Treating device 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.
Acidic Gas Treating device 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.
Acidic Gas Treating device of the present invention, 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.
Acidic Gas Treating device 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 of the present invention and device tool have the following advantages:
1, Acidic Gas Treating process 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 weary gas after Acidic Gas Treating realizes the target of qualified discharge.
2, Acidic Gas Treating process of the present invention, with NaOH solution, MDEA solution biabsorption liquid for absorbent, in reduction system, alkali lye is to CO
2absorption, and ensure H in tail gas
2s content realizes qualified discharge.By adding NaOH alkali lye at second reactor, reduce alkali lye to CO
2the absorption degree of depth, reduce alkali lye to CO
2uptake, fourth-order reaction device adds the biabsorption liquid method of MDEA absorbing liquid, adopts the characteristic that rotary drill reactor gas-liquid contact time is short, utilizes MDEA solvent selectivity to absorb H
2s, improves MDEA selective absorbing H
2the ability of S, ensures purified gas qualified discharge.Reduce CO
2suction rate altogether, makes CO
2major part is stayed in purified gas outside discharger system, thus CO in minimizing system
2overreaction, and product Na
2cO
3, NaHCO
3growing amount, prevent crystallization.
3, Acidic Gas Treating process of the present invention, is rich in Na by what second order reaction obtained
2cO
3the reaction solution of solution enters three reactor as absorbing liquid and uses, and realizes absorbing H further
2s also displaces CO simultaneously
2object, reduce the CO absorbed in sour gas
2, reduce the Na in liquid-phase product
2cO
3, NaHCO
3growing amount, prevent crystallization, assurance device long-term operation.
4, adopt venturi reactor of the present invention as A reactor and second reactor, reaction solution enters reactor liquid phase storage tank 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, Acidic Gas Treating system 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, Acidic Gas Treating process of the present invention, utilizes MDEA solution-selective to absorb H in fourth-order reaction device
2s, reduces CO
2suction rate altogether, takes full advantage of rotary drill reactor efficient mass transfer, the characteristic that gas-liquid contact time is short, improves MDEA solution-selective and absorbs H
2the ability of S, reduces CO
2suction rate altogether.
7, novel acid gas disposal process 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 Acidic Gas Treating process of the present invention and device schematic diagram.
Fig. 2 is the another kind of Acidic Gas Treating process of the present invention and device schematic diagram.
Fig. 3 is venturi reactor schematic diagram in illustrated Acidic Gas Treating process and device.
Detailed description of the invention
Acidic Gas Treating 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, Acidic Gas Treating device shown in the first embodiment of the present invention, described device comprises A reactor 3, second reactor 4, three reactor 6, fourth-order reaction device 8, three grades of pans 7, level Four pans 9, wherein, A reactor 3, second reactor 4, three reactor 6 and fourth-order reaction device 8 arrange gas phase entrance respectively, gaseous phase outlet, liquid phase entrance and liquid-phase outlet, sour gas suction line 1 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 13 through pipeline, clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear 5, the liquid phase entrance of second reactor is connected with alkali liquor inlet pipeline 10, the liquid phase entrance of fourth-order reaction device is connected with MDEA solution inlet pipeline 11, three reactor liquid-phase outlet is point two-way after three grades of pans, one tunnel 19 is connected with three reactor liquid phase entrance, and another road 20 is connected with second reactor liquid phase entrance, second reactor liquid-phase outlet divides three tunnels, and a road 15 is connected with second reactor liquid phase entrance, and a road 16 is connected with A reactor liquid phase entrance, and a road 17 is connected with three reactor liquid phase entrance, A reactor liquid-phase outlet divides two-way, and a road 18 and A reactor liquid phase entrance, a road 14 is connected with product discharge pipeline.
Acidic Gas Treating process of the present invention, first sour gas from sour gas suction line 1 enters A reactor 3, with the generation liquid haptoreaction from second reactor, reaction solution is divided into two-way, wherein a road 18 is connected with A reactor liquid phase entrance, and another road 14 is connected with product discharge pipeline.Sour gas after A reactor process enters second reactor 4, with from the generation liquid of three reactor and NaOH alkali lye haptoreaction, reaction solution is divided into three tunnels, one tunnel generates liquid 16 and enters A reactor as absorbing liquid through A reactor liquid phase entrance, one tunnel generates liquid 15 and enters second reactor, and a road generates liquid 17 and enters three reactor as absorbing liquid.Three reactor 6 is entered through the reacted sour gas of second reactor, generate liquid with second reactor to react, reacted generation liquid enters three grades of pans 7, then divides two-way, the first via 20 enters second reactor through pipeline as absorbing liquid, and the second tunnel 19 loops back three reactor through pipeline; Fourth-order reaction device 8 is entered through the reacted sour gas of three reactor, with the MDEA solution haptoreaction from MDEA solution inlet pipeline 11, through purified gas pipeline 13 qualified discharge after the further demist of reacted sour gas coalescer 2, enter MDEA solution regeneration system after reacted generation liquid enters level Four pans 9, MDEA solution uses through regeneration Posterior circle.
As shown in Figure 2, Acidic Gas Treating device shown in the second embodiment of the present invention, described device comprises A reactor 3, second reactor 4, three reactor 6, fourth-order reaction device 8, three grades of pans 7, level Four pans 9, wherein, A reactor, second reactor divide three sections, 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 1 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 11, clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear 5; The liquid phase entrance of second reactor is connected with alkali liquor inlet pipeline 10, the liquid phase entrance of fourth-order reaction device is connected with MDEA solution inlet pipeline 11, fourth-order reaction device liquid-phase outlet is connected with MDEA solution regeneration system after pans 12, three reactor liquid-phase outlet is point two-way after three grades of pans, one tunnel 19 is connected with three reactor absorbing liquid entrance, and another road 20 is connected with second reactor absorbing liquid entrance; Second reactor liquid-phase outlet divides four tunnels, and a road 15 is connected with second reactor absorbing liquid entrance, and a road 21 is connected with second reactor circulation fluid entrance, and a road 16 is connected with A reactor absorbing liquid entrance, and a road 17 is connected with three reactor absorbing liquid entrance; A reactor liquid-phase outlet divides three tunnels, and a road 18 is connected with A reactor absorbing liquid entrance, and a road 22 is connected with A reactor circulation fluid entrance, and a road 14 is connected with product discharge pipeline.
Acidic Gas Treating process of the present invention, first sour gas from sour gas suction line 1 enters A reactor 3, with the generation liquid haptoreaction from second reactor, reaction solution is divided into three tunnels, wherein a road 18 is connected with A reactor liquid phase entrance, another road 14 is connected with product discharge pipeline, one tunnel 22 is connected with A reactor circulation fluid entrance, wherein, first order reaction generates liquid 22 and enters reactor liquid phase storage tank 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, prevent crystallization.Sour gas after A reactor process enters second reactor 4, with from the generation liquid of three reactor and NaOH alkali lye haptoreaction, reaction solution is divided into four tunnels, the first via generates liquid 16 and enters A reactor as absorbing liquid through A reactor liquid phase entrance, second tunnel generates liquid 15 and enters second reactor, 3rd tunnel generates liquid 17 and enters three reactor, and the 4th tunnel generates liquid 21 and is connected with second reactor circulation fluid entrance; Wherein, the 4th tunnel entering second reactor generates liquid 21 and form downflow weir in second reactor, whole second reactor wall distributes with wall stream form, forming uniform liquid film at reactor wall, take liquid film as division board, not only prevents 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, prevents crystallization.Three reactor 6 is entered through the reacted sour gas of second reactor, generate liquid with second reactor to react, reacted generation liquid enters three grades of pans 7, then divides two-way, the first via 20 enters second reactor through pipeline as absorbing liquid, and the second tunnel 19 loops back three reactor through pipeline; Fourth-order reaction device 8 is entered through the reacted sour gas of three reactor, with the MDEA solution haptoreaction from MDEA solution inlet pipeline 11, through purified gas pipeline 13 qualified discharge after the further demist of reacted sour gas coalescer 21, enter MDEA solution regeneration system after reacted generation liquid enters level Four pans 9, MDEA solution uses through regeneration Posterior circle.
Sour gas comprehensive utilization process 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 (Na
2s, Na
2cO
3, NaHCO
3mixture) react, at H
2when S is excessive, second order reaction generates the Na in liquid
2cO
3, NaHCO
3, Na
2s respectively with H
2s reacts, and generates NaHS solution.The NaHS solution generated divides two-way, and the first via is delivered in finished pot; A reactor is delivered on second road.
(2) course of reaction in second reactor
The main reaction of second reactor is as follows: gas phase is " the weary gas " of first order reaction gas phase, wherein H
2s concentration reduces, but still does not reach discharge standard; Second order reaction liquid phase is that three reactor generates liquid and NaOH solution.Through reaction further, gas phase is purified, and generates certain density Na
2s solution, part is delivered to A reactor and continues reaction as absorbing liquid, and component loops returns second reactor, and some enters fourth-order reaction device as absorbing liquid.
(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.What third-order reaction obtained with second order reaction is rich in Na
2cO
3the reaction solution of solution is absorbing liquid, at H
2when S is a small amount of, Na
2cO
3with H
2s reacts, and generates a small amount of Na
2s, realizes absorbing H
2s replaces CO
2object, reduce the CO absorbed in sour gas
2, reduce the Na in liquid-phase product
2cO
3, NaHCO
3growing amount, prevent crystallization, assurance device long-term operation.
(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, but CO
2content is relatively high.Fourth-order reaction for absorbing liquid, utilizes MDEA solution-selective to absorb H with MDEA solution
2s, reduces CO
2suction rate altogether, takes full advantage of rotary drill reactor efficient mass transfer, the characteristic that gas-liquid contact time is short, improves MDEA solution-selective and absorbs H
2the ability of S, reduces CO
2suction rate altogether.
Below in conjunction with embodiment, reaction effect of the present invention is described, but does not therefore limit the scope of the invention.
Embodiment 1
Adopt processing method as shown in Figure 1 and device, 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 1:2.It is 1:4 that the second order reaction entering three reactor generates the volume flow ratio that liquid and second reactor overall reaction generate liquid.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.The liquid-gas ratio of MDEA solution and sour gas is 10 L/m
3.The mass concentration of MDEA solution is 30%.
In one-level venturi reactor and secondary venturi reactor, reaction temperature is 80 DEG C, and 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.
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 1:3.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 1:6.It is 1:4 that the second order reaction entering three reactor generates the volume flow ratio that liquid and second reactor overall reaction generate liquid.
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.
The liquid-gas ratio of MDEA solution and sour gas is 10 L/m
3.The mass concentration of MDEA solution is 30%.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, for not adopt MDEA solution to absorb, only uses NaOH absorbing liquid.
Table 1 embodiment and comparative example reaction result
Claims (35)
1. an Acidic Gas Treating technique 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 loops back A reactor;
(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 tertiary road, and the first via enters A reactor as absorbing liquid, and the second tunnel loops back second reactor, and the 3rd tunnel enters three reactor as absorbing liquid;
(3) enter three reactor through step (2) reacted sour gas, generate liquid with the 3rd road second reactor and contact and react, reaction solution divides two-way, and the first via enters second reactor, and the second tunnel loops back three reactor;
(4) enter fourth-order reaction device through step (3) reacted sour gas, with MDEA solution reaction, reacted sour gas discharge, reaction solution regeneration Posterior circle uses.
2. according to technique 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 technique 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 1/2 ~ 8/9.
4. according to technique according to claim 1, it is characterized in that: in step (2), entering as absorbing liquid the volume flow ratio that the 3rd road reaction solution of three reactor and second reactor overall reaction generate liquid is 1/6 ~ 1/2, is preferably 1/5 ~ 1/4.
5. according to technique 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.
6. according to technique 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.
7. according to technique according to claim 1, it is characterized in that: the sour gas after step (4) process discharges further after coalescer demist.
8. according to technique 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.
9. according to technique 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.
10. according to technique according to claim 1, it is characterized in that: in three reactor and fourth-order reaction device, reaction temperature is 60 DEG C ~ 90 DEG C, be preferably 65 DEG C ~ 80 DEG C.
11., according to technique according to claim 1, is characterized in that: the liquid-gas ratio of MDEA solution and sour gas is 8L/m
3~ 15L/m
3between, be preferably 10L/m
3~ 12L/m
3.
12. according to technique 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 the technique described in claim 1 or 12, is characterized in that: three reactor, fourth-order reaction device are rotary drill reactor.
14. according to technique 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 technique 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 the technique described in claim 1 or 12, is characterized in that: A reactor, second reactor are venturi reactor.
17., according to technique 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 technique according to claim 17, is characterized in that: the reaction solution that the second tunnel loops back A reactor enters A reactor from circulation fluid entrance and absorbing liquid entrance respectively.
19., according to technique according to claim 18, 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 technique according to claim 17, is characterized in that: the reaction solution that the second tunnel loops back second reactor enters A reactor from circulation fluid entrance and absorbing liquid entrance respectively.
21., according to technique according to claim 20, 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 technique according to claim 17, is characterized in that: described venturi reactor, and 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, are preferably triangle tooth slot structure.
23., according to technique 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 can arrange 1 ~ 10, preferably 4 ~ 6.
24., according to technique 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 technique according to claim 1, is characterized in that: described NaOH solution mass concentration is 20% ~ 60%, are preferably 32% ~ 38%; The mass concentration of MDEA solution is 20% ~ 50%, is preferably 30% ~ 40%.
The sour gas absorption plant of the sour gas absorption technique in 26. employing claims 1 to 25 described in arbitrary claim, it is characterized in that: described device comprises A reactor, second reactor, three reactor, fourth-order reaction device, three grades of pans, level Four pans, 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, clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear, the liquid phase entrance of second reactor is connected with alkali liquor inlet pipeline, and the liquid phase entrance of fourth-order reaction device is connected with MDEA solution inlet pipeline, 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 is connected with A reactor liquid phase entrance, second reactor liquid phase entrance and three reactor liquid phase entrance respectively, A reactor liquid-phase outlet is connected with A reactor liquid phase entrance and product discharge pipeline respectively.
27., according to device according to claim 26, is characterized in that: between fourth-order reaction device gaseous phase outlet and clean gas outlet pipeline, be provided with coalescer, and described coalescer is cylindrical tube, and end socket comprises upper cover and low head, and inside arranges cylindric screen cloth.
28. according to device 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.
29., according to device 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.
30., according to device according to claim 26, is characterized in that: fourth-order reaction device liquid-phase outlet is connected with MDEA regenerative system.
The sour gas absorption plant of the sour gas absorption technique in 31. employing claims 1 to 25 described in arbitrary claim, it is characterized in that: described device comprises A reactor, second reactor, three reactor, fourth-order reaction device, three grades of pans, level Four pans, wherein, A reactor, second reactor are venturi reactor, described venturi reactor divides three sections, 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, clean gas outlet pipeline is provided with hydrogen sulfide content checkout gear; The absorbing liquid entrance of second reactor is connected with alkali liquor inlet pipeline respectively, and fourth-order reaction device absorbing liquid entrance is connected with MDEA solution inlet pipeline; 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 is connected with A reactor absorbing liquid entrance, second reactor absorbing liquid entrance, second reactor circulation fluid entrance respectively and three reactor absorbing liquid entrance connects; A reactor liquid-phase outlet is connected with A reactor circulation fluid entrance, A reactor absorbing liquid entrance and product discharge pipeline respectively.
32., according to device 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.
33., according to device 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.
34., according to device 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.
35., according to device according to claim 31, is characterized in that: fourth-order reaction device liquid-phase outlet is connected with MDEA regenerative system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410046323.4A CN104826464B (en) | 2014-02-10 | 2014-02-10 | Novel acidic gas treating process and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410046323.4A CN104826464B (en) | 2014-02-10 | 2014-02-10 | Novel acidic gas treating process and apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104826464A true CN104826464A (en) | 2015-08-12 |
| CN104826464B CN104826464B (en) | 2017-05-17 |
Family
ID=53804877
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410046323.4A Active CN104826464B (en) | 2014-02-10 | 2014-02-10 | Novel acidic gas treating process and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104826464B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109019955A (en) * | 2018-08-06 | 2018-12-18 | 陈式好 | A kind of petroleum liquid waste treatment system |
| CN113122345A (en) * | 2019-12-30 | 2021-07-16 | 中国石油化工股份有限公司 | System and method for treating high-sulfur natural gas |
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 | Removal method of 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 |
| 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 |
| CN103446849A (en) * | 2013-09-04 | 2013-12-18 | 山东垦利石化集团有限公司 | Separation technology of hydrogen sulfide and carbon dioxide in acid gas of oil refinery |
-
2014
- 2014-02-10 CN CN201410046323.4A patent/CN104826464B/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 | Removal method of 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 |
| 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 |
| CN103446849A (en) * | 2013-09-04 | 2013-12-18 | 山东垦利石化集团有限公司 | Separation technology of hydrogen sulfide and carbon dioxide in acid gas of oil refinery |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109019955A (en) * | 2018-08-06 | 2018-12-18 | 陈式好 | A kind of petroleum liquid waste treatment system |
| CN113122345A (en) * | 2019-12-30 | 2021-07-16 | 中国石油化工股份有限公司 | System and method for treating high-sulfur natural gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104826464B (en) | 2017-05-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104826463B (en) | A kind of sour gas produces NaHS technique and device | |
| CN108722148A (en) | The processing method and processing device of carbonated and hydrogen sulfide gas | |
| CN104826467B (en) | A kind of sour gas prepares NaHS technique and system | |
| CN104826470B (en) | Method and apparatus for treating acidic gas | |
| CN105271132A (en) | SWSR-6 sulfur recovery technology and apparatus thereof | |
| CN104971597B (en) | A kind of sour gas produces NaHS process and device | |
| CN104826464A (en) | Novel acidic gas treating process and apparatus | |
| CN104971601B (en) | Acid gas vertical reactor and processing method | |
| CN104826560B (en) | A kind of sour gas comprehensive utilization process method and system | |
| CN105731497A (en) | Method and apparatus for producing sodium bicarbonate by using acidic gas | |
| CN105727714A (en) | Process and device for production of sodium hydrosulfide | |
| CN105642090A (en) | Acidic gas processing method and apparatus | |
| CN104971600B (en) | A kind of sour gas tubular reactor and handling process method | |
| CN104826465A (en) | Multi-stage countercurrent absorption process and system for acidic gas | |
| CN104826466B (en) | Sour gas three-level counter-current absorption technique and device | |
| CN104826468B (en) | A kind of Acidic Gas Treating technique and system | |
| CN105642091B (en) | A kind of NaHS production technology and device | |
| CN104826469A (en) | Acidic gas countercurrent absorption method and system | |
| CN106345254A (en) | Method and device for treating hydrogen sulfide-containing gas | |
| CN105727715A (en) | Acidic gas treatment process and system | |
| CN105731501A (en) | Method and apparatus for producing solid sodium bicarbonate by using acidic gas | |
| CN104971599B (en) | A kind of sour gas reactor and handling process | |
| CN108722149A (en) | A kind of processing method and processing device of sour gas | |
| CN108722138A (en) | The Acidic Gas Treating technique and system of sulfide hydrogen and carbon dioxide | |
| CN106345135A (en) | Crystallization tower for gas phase reaction |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| EXSB | Decision made by sipo to initiate substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |