CN220968684U - Hydrogen sulfide decomposition hydrogen production equipment - Google Patents
Hydrogen sulfide decomposition hydrogen production equipment Download PDFInfo
- Publication number
- CN220968684U CN220968684U CN202322733083.2U CN202322733083U CN220968684U CN 220968684 U CN220968684 U CN 220968684U CN 202322733083 U CN202322733083 U CN 202322733083U CN 220968684 U CN220968684 U CN 220968684U
- Authority
- CN
- China
- Prior art keywords
- gas
- liquid
- air inlet
- inlet
- absorption tower
- 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.)
- Active
Links
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 229910000037 hydrogen sulfide Inorganic materials 0.000 title claims abstract description 59
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 38
- 239000001257 hydrogen Substances 0.000 title claims abstract description 37
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 238000000354 decomposition reaction Methods 0.000 title description 10
- 239000007788 liquid Substances 0.000 claims abstract description 211
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 82
- 238000002156 mixing Methods 0.000 claims abstract description 79
- 230000003647 oxidation Effects 0.000 claims abstract description 77
- 238000010521 absorption reaction Methods 0.000 claims abstract description 72
- 239000007789 gas Substances 0.000 claims abstract description 70
- 239000007791 liquid phase Substances 0.000 claims abstract description 31
- 239000012071 phase Substances 0.000 claims abstract description 25
- 238000012546 transfer Methods 0.000 claims abstract description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 41
- 239000002245 particle Substances 0.000 claims description 37
- 229910052717 sulfur Inorganic materials 0.000 claims description 34
- 239000011593 sulfur Substances 0.000 claims description 33
- 239000007787 solid Substances 0.000 claims description 28
- 239000000203 mixture Substances 0.000 claims description 18
- 238000005336 cracking Methods 0.000 claims description 13
- 239000002002 slurry Substances 0.000 claims description 10
- 238000000197 pyrolysis Methods 0.000 claims description 6
- 239000012295 chemical reaction liquid Substances 0.000 claims description 5
- 239000005864 Sulphur Substances 0.000 claims description 4
- 238000005868 electrolysis reaction Methods 0.000 claims description 3
- 239000006260 foam Substances 0.000 claims 1
- 239000012530 fluid Substances 0.000 abstract description 5
- 230000003993 interaction Effects 0.000 abstract description 5
- 239000007790 solid phase Substances 0.000 abstract description 4
- 238000006243 chemical reaction Methods 0.000 description 24
- 238000000034 method Methods 0.000 description 16
- 230000001590 oxidative effect Effects 0.000 description 12
- 238000007599 discharging Methods 0.000 description 9
- 238000001179 sorption measurement Methods 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 239000002253 acid Substances 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 5
- 150000002431 hydrogen Chemical class 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000007800 oxidant agent Substances 0.000 description 4
- 239000006096 absorbing agent Substances 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000007547 defect Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- -1 polytetrafluoroethylene Polymers 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- WHBHBVVOGNECLV-OBQKJFGGSA-N 11-deoxycortisol Chemical compound O=C1CC[C@]2(C)[C@H]3CC[C@](C)([C@@](CC4)(O)C(=O)CO)[C@@H]4[C@@H]3CCC2=C1 WHBHBVVOGNECLV-OBQKJFGGSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005536 corrosion prevention Methods 0.000 description 1
- 210000003298 dental enamel Anatomy 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002848 electrochemical method Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 230000001699 photocatalysis Effects 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 239000002341 toxic gas Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses hydrogen production equipment by decomposing hydrogen sulfide, which relates to the technical field of hydrogen sulfide treatment equipment and comprises a gas-liquid mixer, an oxidation absorption tower, a solid-liquid separator and an electrolytic tank, wherein the feed end of the gas-liquid mixer is respectively connected and communicated with the output ends of an oxidation liquid circulation line and a mixed gas conveying line containing hydrogen sulfide, a first gas-liquid mixing air inlet, a second gas-liquid mixing air inlet and a third gas-liquid mixing air inlet are arranged on the oxidation absorption tower, and the angles between the axes of the discharge ends of the first gas-liquid mixing air inlet, the second gas-liquid mixing air inlet and the third gas-liquid mixing air inlet and the central axis of the oxidation absorption tower are respectively 13-15 ℃, 15-17 ℃ and 45-47 ℃. The utility model further converts the hydrogen sulfide which is not absorbed by the absorption reactor, reduces the adhesion of a solid phase, mixes by means of fluid interaction, increases the contact area of gas phase and liquid phase, and improves the mass transfer efficiency.
Description
Technical Field
The utility model relates to the technical field of hydrogen sulfide treatment equipment, in particular to hydrogen production equipment by decomposing hydrogen sulfide.
Background
Hydrogen sulfide is a toxic gas with great hazard produced in petroleum, natural gas and petrochemical industries, most enterprises adopt the claus method for treatment, and the main purpose is to recover sulfur in the hydrogen sulfide, wherein the hydrogen generates water through oxidation. In recent years, the country has promoted the utilization of hydrogen energy greatly, and how to change the hydrogen element in hydrogen sulfide into hydrogen energy is a popular subject for domestic and foreign research. Hydrogen sulfide can be produced by the technologies of microwave method decomposition, catalytic thermal decomposition, photocatalytic decomposition and the like, and the method is limited in experimental stage and has no industrial trend. The technology for preparing hydrogen from hydrogen sulfide by using an indirect electrochemical method is mature gradually, the technology can be expanded and popularized, and meanwhile, the technology has some defects, and the technology is further perfection for preparing hydrogen from hydrogen sulfide.
The technology firstly utilizes gaseous hydrogen sulfide and liquid phase oxidant to produce solid sulfur, the reaction is carried out in an oxidation reaction vessel, the hydrogen sulfide conversion rate is 85-90%, and three phases of gas, liquid and solid exist simultaneously in the reaction process. The oxidant is in a liquid phase and is usually prepared by adopting a Fe 2(SO4)3+H2SO4 solution, H 2 S is oxidized by an oxidizing solution containing Fe 3+ in an absorption reactor to generate sulfur particles, meanwhile Fe 3+ is reduced to Fe 2+, slurry containing sulfur particles is sent to a solid-liquid separator, after sulfur is removed, the solution containing H + and Fe 2+ is sent to an electrolysis reactor, fe 2+ is oxidized to Fe 3+ at an anode and then sent back to the absorption reactor for recycling, and H + passes through an ion exchange membrane to enter a cathode to be reduced to H 2 and is released from the cathode.
The reaction of the whole process is as follows:
Fe in absorption reactor 2(SO4)3+H2S＝2FeSO4+S↓+H2SO4
Ion equation: 2Fe 3++H2S＝2Fe2+ +2H++ S +.
Electrolytic reaction tank reaction of FeSO 4+H2SO4+＝Fe2(SO4)3+H2 ≡
Ion equation: 2Fe 2++2H+＝2Fe3++H2 ≡
The total reaction of the whole process is H 2S＝S↓+H2 ≡
The technological process mainly comprises two parts of elemental sulfur produced by an absorption reactor and hydrogen produced by an electrolytic cell. The main problem is firstly that hydrogen sulphide cannot be completely converted into hydrogen and sulphur, and the conversion is low.
And secondly, the corrosion and blockage of the absorption reactor are serious. The oxidation medium contains strong acid radicals, so that the oxidation medium has strong corrosiveness, and the oxidation medium has an important function in the technology how to select materials to avoid corrosion. For the container with gas, liquid and solid phases simultaneously, the internal structure is also very important, solid sulfur particles generated in the oxidation process are easy to aggregate and are attached to tower internals such as inlet and outlet pipes, tower inner walls, packing layers, gas-liquid distribution plates and the like to block the container. The oxidation process of H 2 S is a fast reaction process controlled by mass transfer, the design of the reactor can prevent corrosion, and the production capacity of the whole process can be improved by avoiding blockage.
Conventional oxidizers include packed columns, bubble columns, stirred mixing columns, and the like. When solid sulfur is generated, the packed tower is easy to cause channel blockage and cannot be operated; the bubbling tower has small gas-liquid mass transfer area and low mass transfer efficiency, and solid products generated in the oxidation process are easy to block a gas distributor to influence the distribution of gas, and the mixing tower with stirring has strong acid roots due to the oxidation liquid, so that the components such as a transmission shaft, a bearing, a seal and the like are severely corroded. These drawbacks make conventional absorber towers unusable for long periods of time.
The internal circulation type absorption reactor disclosed in patent publication No. CN100450917C has a relatively complex internal structure and relatively high manufacturing and maintenance costs. When the gap distance between the inner pipe and the sleeve is larger, the gas and the liquid cannot be mixed, and when the gap distance is smaller, solid sulfur can be attached to the pipe wall, so that the pipe is blocked. From the aspect of chemical structure, the gas phase that the inner tube comes out can not totally turn up, and a part directly comes out from the bottom, and the resistance that comes out from the bottom is less than the resistance that turns up, can not reach the purpose of gas-liquid mixture.
The jet type absorption reactor with the patent publication No. CN107537301B is only suitable for laboratories, and when the reaction scale is enlarged, the defects of uneven mixing, stringing of air flow, reduced efficiency and the like can occur.
Accordingly, one skilled in the art would be able to provide a hydrogen sulfide decomposition hydrogen production plant that addresses the problems set forth in the background above.
Disclosure of utility model
The utility model provides a method for improving the conversion rate of hydrogen sulfide, adding a high-temperature cracking reactor, further converting the hydrogen sulfide which is not absorbed by an absorption reactor, modifying the absorption reactor, reducing the adhesion of a solid phase, and avoiding the problems of equipment corrosion, poor reaction stability, low efficiency and the like caused by the blockage of a tower body and pipe fitting sulfur; the hydrogen production equipment for decomposing hydrogen sulfide is characterized in that the contact area of gas phase and liquid phase is increased by mixing under the interaction of fluid, and the mass transfer efficiency is improved.
In order to achieve the above object, the present utility model provides the following technical solutions:
the utility model relates to hydrogen sulfide decomposition hydrogen production equipment, which comprises the following components:
The gas-liquid mixer is respectively connected with the feeding end of the gas-liquid mixer and is communicated with the output end of the oxidation liquid circulating line and the output end of the mixed gas conveying line containing hydrogen sulfide, and the diameters of the top end and the bottom end of the gas-liquid mixer are larger than the diameter of the middle part;
The oxidation absorption tower is provided with a first gas-liquid mixing air inlet, a second gas-liquid mixing air inlet and a third gas-liquid mixing air inlet, the first gas-liquid mixing air inlet, the second gas-liquid mixing air inlet and the third gas-liquid mixing air inlet are all arranged along the outer wall of the oxidation absorption tower, the first gas-liquid mixing air inlet, the second gas-liquid mixing air inlet and the third gas-liquid mixing air inlet are positioned on the same plane, the first gas-liquid mixing air inlet, the second gas-liquid mixing air inlet and the third gas-liquid mixing air inlet are communicated with the discharge end of the gas-liquid mixer through a conveying pipeline, and the angles between the axes of the discharge ends of the first gas-liquid mixing air inlet, the second gas-liquid mixing air inlet and the third gas-liquid mixing air inlet and the central axis of the oxidation absorption tower are respectively 13-15 ℃, 15-17 ℃ and 45-47 ℃;
The solid-liquid separator is used for separating sulfur from reaction liquid, the feeding end of the solid-liquid separator is communicated with a liquid phase outlet containing solid particles at the bottom of the oxidation absorption tower through a conveying pipeline, a conveying pump is arranged on the conveying pipeline, liquid containing light sulfur particles is arranged at the upper part of the liquid level of the oxidation absorption tower, and slurry of the light sulfur particles is conveyed to the solid-liquid separator through the conveying pipeline;
The feeding end of the electrolytic tank is connected with the top discharging end of the solid-liquid separator through a conveying pipeline, the electrolytic tank receives clear liquid conveyed by the solid-liquid separator, the electrolytic tank electrolyzes the clear liquid to produce hydrogen, and the rest oxidizing liquid after the electrolytic tank is electrolyzed is returned to the gas-liquid mixer through an oxidizing liquid circulating line.
Further, the other liquid phase outlet containing solid particles of the oxidation absorption tower is communicated with the feeding end of the conveying pump, the other liquid phase outlet containing solid particles is arranged above the plane where the first gas-liquid mixing air inlet, the second gas-liquid mixing air inlet and the third gas-liquid mixing air inlet are located, and the slurry containing heavier particles is conveyed to the solid-liquid separator from the liquid phase outlet containing solid particles at the lower part of the oxidation absorption tower.
Further, a wire mesh demister is arranged at the top of the oxidation absorption tower and is positioned above the other liquid phase outlet containing solid particles; the third discharge end of the oxidation absorption tower is communicated with the gas-liquid separator through a tower top gas phase line, and the wire mesh demister is positioned below another liquid phase outlet containing solid particles; the gas after the oxidation reaction in the oxidation absorption tower passes through a wire mesh demister and is conveyed to a gas-liquid separator by a tower top gas phase line, and mist carried by the gas is removed by the wire mesh demister.
Further, the bottom discharge end of the gas-liquid separator is communicated with the other feed end of the solid-liquid separator through a conveying pipeline.
Further, the other discharging end of the gas-liquid separator is respectively communicated with a first inlet, a second inlet and a third inlet through a gas-phase circulation line of an induced draft fan, the first inlet, the second inlet and the third inlet are positioned below planes where the first gas-liquid mixing air inlet, the second gas-liquid mixing air inlet and the third gas-liquid mixing air inlet are positioned, the first inlet, the second inlet and the third inlet are all arranged along the outer wall of the oxidation absorption tower, and the first inlet, the second inlet and the third inlet are positioned on the same plane; the insufficiently oxidized hydrogen sulfide separated by the gas-liquid separator is conveyed to an oxidation absorption tower for secondary oxidation through a gas-phase circulation line of an induced draft fan, so that the content of the hydrogen sulfide of the discharged gas is less than or equal to 15-10%; bubbling in different directions through the first inlet, the second inlet and the third inlet, so as to prevent sulfur settled at the bottom from forming a block and generating blockage.
Further, the top discharge end of the gas-liquid separator is communicated with the feed end of the pyrolysis furnace.
Further, the discharge end of the high-temperature cracking furnace is communicated with the feed end of the condenser through a conveying pipeline, and the temperature of the high-temperature cracking furnace is 1150-1200 ℃.
Further, the condenser is used for conveying the converted liquid to the catcher through the conveying pipeline, the catcher is used for separating liquid sulfur, and the output end of the catcher is communicated with the feeding end of the pressure swing absorption tank through the mixed gas line.
Further, the pressure swing absorption box receives the gas transmitted by the catcher, and divides the waste gas and the hydrogen gas, and the waste gas is burnt.
In the technical scheme, the hydrogen sulfide decomposition hydrogen production equipment provided by the utility model has the following beneficial effects:
1. The conversion rate of the hydrogen sulfide is improved, a high-temperature cracking reactor is added, the unabsorbed hydrogen sulfide is further converted, and the technical process of hydrogen production by decomposing the hydrogen sulfide is improved.
2. The adhesion of solid phase is reduced, and the problems of equipment corrosion, poor reaction stability, low efficiency and the like caused by the blockage of the tower body and pipe fitting sulfur of the oxidation absorption tower are avoided. The mixing is carried out by means of fluid interaction, so that the contact area of the gas phase and the liquid phase is increased, and the mass transfer efficiency is improved.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings required for the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments described in the present utility model, and other drawings may be obtained according to these drawings for a person having ordinary skill in the art.
FIG. 1 is a schematic diagram of a hydrogen sulfide decomposition hydrogen production plant according to an embodiment of the present utility model;
FIG. 2 is a cross-sectional view of the first gas-liquid mixture inlet portion of the oxidation absorber of FIG. 1;
FIG. 3 is a cross-sectional view of a first inlet location on the oxidation absorber of FIG. 1.
In the figure:
1. A gas-liquid mixer; 2. an oxidation absorption tower; 3. a solid-liquid separator; 4. an electrolytic cell; 5. a pyrolysis furnace; 6. a condenser; 7. a catcher; 8. a variable pressure absorption box; 9. a gas-liquid separator;
101. An oxidizing liquid circulation line; 102. a mixed gas delivery line;
201. A first gas-liquid mixing inlet; 202. a second gas-liquid mixing inlet; 203. a third gas-liquid mixing inlet; 204. a liquid phase outlet containing solid particles; 206. a wire mesh demister; 207. a top gas phase line; 208. a first inlet; 209. a second inlet; 210. a third inlet;
301. a transfer pump;
401. a gas phase circulation line of the induced draft fan;
701. And a mixed gas line.
Detailed Description
In order to make the technical scheme of the present utility model better understood by those skilled in the art, the present utility model will be further described in detail with reference to the accompanying drawings.
See fig. 1-3;
the hydrogen sulfide decomposition hydrogen production equipment provided by the embodiment of the utility model comprises:
The gas-liquid mixer 1, the feed end of the gas-liquid mixer 1 is respectively connected and communicated with the output ends of the oxidation liquid circulation line 101 and the mixed gas conveying line 102 containing hydrogen sulfide, and the diameters of the top end and the bottom end of the gas-liquid mixer 1 are larger than the diameter of the middle part;
The oxidation absorption tower 2, a first gas-liquid mixing air inlet 201, a second gas-liquid mixing air inlet 202 and a third gas-liquid mixing air inlet 203 are arranged on the oxidation absorption tower 2, the first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet 203 are all arranged along the outer wall of the oxidation absorption tower 2, the first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet 203 are located on the same plane, the first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet 203 are communicated with the discharging end of the gas-liquid mixer 1 through a conveying pipeline, and the angles between the axes of the discharging ends of the first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet 203 and the central axis of the oxidation absorption tower 2 are respectively 13-15 ℃, 15-17 ℃, 45-47 ℃, preferably 14 ℃, 16 ℃ and 46 ℃;
A solid-liquid separator 3, wherein the solid-liquid separator 3 separates sulfur and reaction liquid, the feed end of the solid-liquid separator 3 is communicated with a liquid phase outlet 204 containing solid particles at the bottom of the oxidation absorption tower 2 through a conveying pipeline, a conveying pump 301 is arranged on the conveying pipeline, the liquid containing light sulfur particles is arranged at the upper part of the liquid surface of the oxidation absorption tower 2, and slurry of the light sulfur particles is conveyed to the solid-liquid separator 3 through the conveying pipeline;
The feeding end of the electrolytic tank 4 is connected with the top discharging end of the solid-liquid separator 3 through a conveying pipeline, the electrolytic tank 4 receives clear liquid conveyed by the solid-liquid separator 3, the electrolytic tank 4 electrolyzes the clear liquid to produce hydrogen, and residual oxidation liquid after the electrolysis of the electrolytic tank 4 is returned to the gas-liquid mixer 1 through the oxidation liquid circulating line 101.
The other solid particle-containing liquid phase outlet 204 of the oxidation absorption tower 2 is communicated with the feeding end of the conveying pump 301, the other solid particle-containing liquid phase outlet 204 is arranged above the plane where the first gas-liquid mixing gas inlet 201, the second gas-liquid mixing gas inlet 202 and the third gas-liquid mixing gas inlet 203 are located, and the slurry containing heavier particles is conveyed from the solid particle-containing liquid phase outlet 204 at the lower part of the oxidation absorption tower 2 to the solid-liquid separator 3. A wire mesh demister 206 is arranged at the top of the oxidation absorption tower 2, and the wire mesh demister 206 is positioned above another liquid phase outlet 204 containing solid particles; the third discharging end of the oxidation absorption tower 2 is communicated with the gas-liquid separator 9 through a tower top gas phase line 207, and the wire mesh demister 206 is positioned below another liquid phase outlet 204 containing solid particles; the gas after the oxidation reaction in the oxidation absorption tower 2 passes through a wire mesh demister 206 and is conveyed to the gas-liquid separator 9 by a tower top gas phase line 207, and mist carried by the gas is removed by the wire mesh demister 206.
The bottom discharge end of the gas-liquid separator 9 is communicated with the other feed end of the pyrolysis furnace 5 through a conveying pipeline. The other discharging end of the gas-liquid separator 9 is respectively communicated with a first inlet 208, a second inlet 209 and a third inlet 210 through a gas-phase circulation line 401 of an induced draft fan, the first inlet 208, the second inlet 209 and the third inlet 210 are positioned below a plane where the first gas-liquid mixing gas inlet 201, the second gas-liquid mixing gas inlet 202 and the third gas-liquid mixing gas inlet 203 are positioned, the first inlet 208, the second inlet 209 and the third inlet 210 are all arranged along the outer wall of the oxidation absorption tower 2, and the first inlet 208, the second inlet 209 and the third inlet 210 are positioned on the same plane; the insufficiently oxidized hydrogen sulfide separated by the gas-liquid separator 9 is conveyed to the oxidation absorption tower 2 for re-oxidation through a gas-phase circulation line 401 of an induced draft fan, so that the content of the hydrogen sulfide of the discharged gas is less than or equal to 15-10%; bubbling in different directions through the first inlet, the second inlet and the third inlet, so as to prevent sulfur settled at the bottom from forming a block and generating blockage.
The top discharge end of the gas-liquid separator 9 is communicated with the feed end of the pyrolysis furnace 5. The discharge end of the high-temperature cracking furnace 5 is communicated with the feed end of the condenser 6 through a conveying pipeline, and the temperature of the high-temperature cracking furnace 5 is 1150-1200 ℃. The condenser 6 conveys the converted liquid to the catcher 7 through a conveying pipeline, the catcher 7 separates out liquid sulfur, and the output end of the catcher 7 is communicated with the feeding end of the pressure swing absorption tank 8 through a mixed gas line 701. The pressure swing absorption box 8 receives the gas transmitted by the catcher 7, and divides the exhaust gas and the hydrogen gas, and the exhaust gas is burnt.
The utility model also provides a method for producing hydrogen by decomposing hydrogen sulfide, which comprises the following specific processes (see figure 1):
Firstly, preparing an oxidant A solution by using Fe 2(SO4)3 and H 2SO4 solutions according to a certain proportion, mixing the oxidant A solution with a mixed gas B containing H 2 S through a gas-liquid mixer 1, wherein the mixed gas containing H 2 S is generally derived from refinery acid gas and natural gas of an oil-gas field, the concentration of H 2 S in the mixed gas B is preferably 0.5-80%, the gas-liquid mixer 1 is small in diameter at the middle part of two ends, and when the gas-liquid fluid is changed from a large-diameter horn-shaped channel to a small-diameter channel, the flow speed is rapidly increased, and the gas-liquid two phases are sprayed out from a neck-shrinking opening in the middle part of the gas-liquid mixer 1 at a high speed;
In the second step, fluid sprayed from the gas-liquid mixer 1 at high speed is divided into three paths in the same radial direction and enters the oxidation absorption tower 2 through the first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet 203, the axes of the first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet 203 and the central axis of the oxidation absorption tower 2 are respectively 13-15 ℃, 15-17 ℃ and 45-47 ℃, the purpose is that liquid phases sprayed from the first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet 203 are in a triangular shape, three gas-liquid collision and interaction (shown in fig. 2) push the oxidation reaction liquid to rotate clockwise, fe 3+ and H 2 S react to generate Fe 2+ and S, H + are free to exist in the form of H 2SO4, the better gas-liquid mixing reaction is faster, elementary substance S is formed in the liquid phase, light-weight elementary substance sulfur particles float up along with the air flow, are accumulated on the upper part of the tower, and heavy elementary substance sulfur is sunk into the bottom of the oxidation absorption tower 2.
Thirdly, discharging slurry of light sulfur particles accumulated on the upper part of the oxidation absorption tower 2 through a liquid phase outlet 204 pipeline containing solid particles, discharging slurry containing heavier particles from the lower part of the tower through the liquid phase outlet 204 pipeline containing solid particles, conveying the slurry to a solid-liquid separator 3 through a conveying pump 301, precipitating the solid sulfur in the solid-liquid separator 3, centrifuging and separating the sulfur from reaction liquid;
Fourthly, after solid sulfur is separated out in the solid-liquid separator 3, clear liquid enters the electrolytic tank 4, electrons are obtained from the H + to the cathode in the electrolytic tank 4 and become H 2 to be separated out, liquid Fe 2+ is reduced into Fe 3+ at the anode in a power-off way and is converted into oxidizing liquid, and the oxidizing liquid returns to the gas-liquid mixer 1 for repeated use in the form of Fe 2(SO4)3 through the oxidizing liquid circulating line 101;
Fifthly, the oxidized gas is ejected out through an oxidation absorption tower 2, the conversion rate of hydrogen sulfide is 85-90%, the oxidized gas enters a gas-liquid separator 9 through a wire mesh demister 206 at the top of the tower from a tower top gas phase line 207, mist carried by the gas is mainly removed by the wire mesh demister 206, a large amount of liquid carried by the gas is separated by the gas-liquid separator 9, and the gas returns to a solid-liquid separator 3;
Step six, a gas phase circulation line 401 of a draught fan with 1/4 to 1/5 of the gas discharged from the gas-liquid separator 9 is divided into three paths to enter the oxidation absorption tower 2 for recirculation through a first inlet 208, a second inlet 209 and a third inlet 210, firstly, hydrogen sulfide which is insufficiently oxidized is oxidized again, and the content of hydrogen sulfide in discharged gas is ensured to be less than or equal to 15 to 10 percent; secondly, the three air inlet pipes bubble along different directions to prevent sulfur settled at the bottom from forming a block and blocking;
Seventh, the gas coming out from the top of the gas-liquid separator 9 enters a high-temperature cracking furnace 5, the temperature is preferably 1150-1200 ℃, oxygen is isolated from the furnace to prevent S from oxidizing, the hydrogen sulfide which is not absorbed in the equipment is decomposed at high temperature to generate gas-phase sulfur and hydrogen, so as to improve the conversion rate of the hydrogen sulfide, the high-temperature cracking furnace 5 is suitable for the condition of low concentration of the hydrogen sulfide, the content of the hydrogen sulfide is less than or equal to 5 percent, the concentration of the hydrogen sulfide is low, the reaction is thorough, and the conversion rate is high;
eighth, after the gas-phase sulfur and the hydrogen are cooled by the condenser 6, the gas-phase sulfur is changed into a liquid phase, the liquid phase sulfur enters the catcher 7 to form liquid sulfur to flow out, the gas-phase part enters the pressure swing adsorption box 8 through the mixed gas line 701, adsorbents are arranged in the pressure swing adsorption box 8, the adsorbents have different adsorption capacity, adsorption speed and adsorption force on different gases, and the pressure swing adsorption selects different adsorbents according to the characteristics of the hydrogen to realize the hydrogen separation;
And step nine, hydrogen is separated from other mixed gases through pressure swing adsorption to become pure hydrogen, the other gases are burnt in an incinerator and are discharged after alkali liquor treatment, and the mixed gas containing H 2 S is generally obtained from oil-gas fields and petrochemical industry and contains N 2、CO、CO2、O2, part of organic sulfur and the like to be burnt.
The hydrogen sulfide in the above process is reacted twice, and is oxidized by strong acid for the first time, S 2- is oxidized into elemental sulfur in the device of the application, and H + is reduced into H 2 in the electrolytic tank 4. In the reaction process, 10-15% of mixed gas H 2 S is unreacted, and the rest H 2 S enters a cracking furnace and belongs to the second reaction, and direct pyrolysis is carried out: h 2S＝S+H2, the content of hydrogen sulfide in the final exhaust gas is less than or equal to 0.5-0.1%, the high-temperature cracking decomposition reaction is severe in reaction conditions, the reverse reaction exists, rapid condensation is needed, and the method is suitable for decomposing low-concentration hydrogen sulfide.
In the first reaction process, the oxidation absorption tower 2 is an important device, and because the oxidation solution is Fe 2(SO4)3+H2SO4 solution or FeCI 3 +HC I solution, the oxidation absorption tower has strong corrosiveness, the device adopts a graphite-lined polytetrafluoroethylene material, lead is lined and enamel is used, the applicable temperature is 0 to +150 ℃, and the oxidation absorption tower can resist 500 to 800Kpa.
The filler in the wire mesh demister 206 is acid-resistant phenolic, polyethylene or other nonmetallic material. The first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet are arranged on the same horizontal plane, the central line of the pipe is at different angles with the axis of the oxidation absorption tower 2, the first gas-liquid mixing air inlet 201, the second gas-liquid mixing air inlet 202 and the third gas-liquid mixing air inlet are contracted inwards, liquid is discharged to form a jet flow, the liquid is in a regular triangle state, all paths of gas-liquid collision each other, the gas bubbles are thinned and become small, the gas bubbles are fully mixed into the liquid, the liquid in the oxidation absorption tower 2 is pushed to slowly rotate along the clockwise direction, and hydrogen sulfide is fully converted into elemental sulfur in the process of rotating and rising from the bottom of the oxidation absorption tower 2.
The induced draft fan gas phase circulation line 401 increases the efficiency of hydrogen sulfide oxidation, the outlet ends of the first inlet 208, the second inlet 209 and the third inlet 210 are respectively sprayed with bubbles along the radial direction and the circumferential direction, and float up from the bottom along the tower after interaction, and hydrogen sulfide in the oxidation absorption tower 2 is returned to be fully oxidized.
The inside of the whole oxidation absorption tower 2 is basically free of accessories, so that the adsorption blockage of elemental sulfur particles is prevented, and the corrosion prevention implementation is also facilitated.
The gas-liquid mixer 1 of the tower oxidation absorption tower 2 is a container with two ends in a horn mouth shape and an inside necking, and a spiral guide plate is arranged in the horn mouth of the outlet end, and the gas-liquid is rotated at a high speed after coming out.
While certain exemplary embodiments of the present utility model have been described above by way of illustration only, it will be apparent to those of ordinary skill in the art that modifications may be made to the described embodiments in various different ways without departing from the spirit and scope of the utility model. Accordingly, the drawings and description are to be regarded as illustrative in nature and not as restrictive of the scope of the utility model, which is defined by the appended claims.
Claims (8)
1. A hydrogen sulfide decomposing hydrogen production plant, characterized by comprising:
The device comprises a gas-liquid mixer (1), wherein the feeding end of the gas-liquid mixer (1) is respectively connected and communicated with the output ends of an oxidation liquid circulation line (101) and a mixed gas conveying line (102) containing hydrogen sulfide, and the diameters of the top end and the bottom end of the gas-liquid mixer (1) are larger than the diameter of the middle part;
The oxidation absorption tower (2), be provided with first gas-liquid mixture air inlet (201), second gas-liquid mixture air inlet (202) and third gas-liquid mixture air inlet (203) on oxidation absorption tower (2), first gas-liquid mixture air inlet (201), second gas-liquid mixture air inlet (202) and third gas-liquid mixture air inlet (203) are all set up along the outer wall of oxidation absorption tower (2), and first gas-liquid mixture air inlet (201), second gas-liquid mixture air inlet (202) and third gas-liquid mixture air inlet (203) are located the coplanar, first gas-liquid mixture air inlet (201), second gas-liquid mixture air inlet (202) and third gas-liquid mixture air inlet (203) are through pipeline and the discharge end intercommunication of gas-liquid mixture (1), the angle between the axis of the discharge end of first gas-liquid mixture air inlet (201), second gas-liquid mixture air inlet (202) and third gas-liquid mixture air inlet (203) and the axis of oxidation absorption tower (2) is 13-15 ℃, 15-17 ℃, 45-47 ℃ respectively;
The solid-liquid separator (3), the solid-liquid separator (3) separates sulphur and reaction liquid, the feed end of the solid-liquid separator (3) is communicated with a liquid phase outlet (204) containing solid particles at the bottom of the oxidation absorption tower (2) through a conveying pipeline, a conveying pump (301) is arranged on the conveying pipeline, the liquid containing light sulphur particles is arranged at the upper part of the liquid surface of the oxidation absorption tower (2), and the slurry of the light sulphur particles is conveyed to the solid-liquid separator (3) through the conveying pipeline;
The electrolytic tank (4), the feed end of electrolytic tank (4) is connected through transfer line with the top discharge end of solid-liquid separator (3), the clear solution that solid-liquid separator (3) carried is accepted to electrolytic tank (4), and electrolytic tank (4) goes out hydrogen to the clear solution, and the oxidation liquid that remains after electrolytic tank (4) electrolysis is passed back through oxidation liquid circulation line (101) gas-liquid mixer (1).
2. A hydrogen sulfide decomposing hydrogen production device as defined in claim 1, wherein: the other liquid phase outlet (204) containing solid particles of the oxidation absorption tower (2) is communicated with the feeding end of the conveying pump (301), the other liquid phase outlet (204) containing solid particles is arranged above the plane where the first gas-liquid mixing gas inlet (201), the second gas-liquid mixing gas inlet (202) and the third gas-liquid mixing gas inlet (203) are arranged, and slurry containing heavier particles is conveyed to the solid-liquid separator (3) from the liquid phase outlet (204) containing solid particles at the lower part of the oxidation absorption tower (2).
3. A hydrogen sulfide decomposing hydrogen production device as defined in claim 1, wherein: a wire mesh demister (206) is arranged at the top of the oxidation absorption tower (2), and the wire mesh demister (206) is positioned above another liquid phase outlet (204) containing solid particles; the third discharge end of the oxidation absorption tower (2) is communicated with the gas-liquid separator (9) through a tower top gas phase line (207), and the wire mesh foam remover (206) is positioned below another liquid phase outlet (204) containing solid particles.
4. A hydrogen sulfide decomposing hydrogen production plant as claimed in claim 3, characterized in that: the bottom discharge end of the gas-liquid separator (9) is communicated with the other feed end of the pyrolysis furnace (5) through a conveying pipeline.
5. A hydrogen sulfide decomposing hydrogen production device as defined in claim 4, wherein: the other discharge end of the gas-liquid separator (9) is respectively communicated with a first inlet (208), a second inlet (209) and a third inlet (210) through a gas-phase circulation line (401) of an induced draft fan, the first inlet (208), the second inlet (209) and the third inlet (210) are positioned below the plane where the first gas-liquid mixing air inlet (201), the second gas-liquid mixing air inlet (202) and the third gas-liquid mixing air inlet (203) are positioned, and the first inlet (208), the second inlet (209) and the third inlet (210) are all arranged along the outer wall of the oxidation absorption tower (2), and the first inlet (208), the second inlet (209) and the third inlet (210) are positioned on the same plane.
6. A hydrogen sulfide decomposing hydrogen production device as defined in claim 5, wherein: the top discharge end of the gas-liquid separator (9) is communicated with the feed end of the high-temperature cracking furnace (5).
7. A hydrogen sulfide decomposing hydrogen production device as defined in claim 6, wherein: the discharge end of the high-temperature cracking furnace (5) is communicated with the feed end of the condenser (6) through a conveying pipeline, and the temperature of the high-temperature cracking furnace (5) is 1150-1200 ℃.
8. A hydrogen sulfide decomposing hydrogen production device as defined in claim 7, wherein: the condenser (6) is used for conveying the converted liquid to the catcher (7) through a conveying pipeline, the catcher (7) is used for separating liquid sulfur, and the output end of the catcher (7) is communicated with the feeding end of the pressure swing absorption box (8) through a mixed gas line (701).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322733083.2U CN220968684U (en) | 2023-10-11 | 2023-10-11 | Hydrogen sulfide decomposition hydrogen production equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322733083.2U CN220968684U (en) | 2023-10-11 | 2023-10-11 | Hydrogen sulfide decomposition hydrogen production equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220968684U true CN220968684U (en) | 2024-05-17 |
Family
ID=91062247
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322733083.2U Active CN220968684U (en) | 2023-10-11 | 2023-10-11 | Hydrogen sulfide decomposition hydrogen production equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220968684U (en) |
-
2023
- 2023-10-11 CN CN202322733083.2U patent/CN220968684U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN203612955U (en) | Liquid sulfur degassing device | |
| CN106731632A (en) | The device and its technique of a kind of zinc oxide removing sulfur dioxide in flue gas | |
| CN102476893B (en) | Biological desulphurization processing reactor, biological desulphurization processing system, and processing method | |
| CN102716657A (en) | Zinc oxide desulfurization method applicable to zinc smelting system | |
| CN220968684U (en) | Hydrogen sulfide decomposition hydrogen production equipment | |
| CN111514716B (en) | Flue gas desulfurization, denitrification and demercuration purification method and equipment | |
| CN104667726A (en) | Device and method for purifying in treatment of volatile gas of petrochemical coke cooling water tank | |
| CN204412040U (en) | A kind of combined type Gas Purification Factory low concentration acid gas processing device | |
| CN106853328A (en) | A kind of hydrogen peroxide Efficient utilization method and device for low-temperature flue gas desulphurization denitration | |
| CN202575972U (en) | Chlorine dioxide reaction device | |
| CN103193371B (en) | Method and device for sludge oxidation by supercritical water | |
| CN114671766A (en) | Method for preparing nitrobenzoic acid by intersection type continuous oxidation | |
| CN115894400A (en) | Process for preparing epoxy chloropropane by directly oxidizing chloropropene by using liquid-solid circulating fluidized bed reactor | |
| CN205710313U (en) | A kind of wiring board alkali etching ammonia nitrogen wastewater treatment device | |
| CN212881806U (en) | Flue gas desulfurization, denitrification and demercuration purification equipment | |
| CN107569998A (en) | A kind of mine tailing smelts three wastes desulphurization system and method | |
| CN108217606A (en) | Utilize the cross-flow moving bed device of carbon-based material reduction and desulfurization resolution gas Recovered sulphur | |
| CN210645857U (en) | Ammonia desulphurization oxidation device | |
| CN210710748U (en) | Liquid sulfur pool air exhaust and liquid sulfur degassing combined device | |
| CN206858249U (en) | Electrode couples ozone oxidation all-in-one fluidization bed reactor | |
| CN101456596B (en) | Reactor suitable for sulphur dioxide gas leach manganese dioxide ore | |
| CN111760422B (en) | Variable-flow turbulent bubble type pre-absorption process for removing sulfur dioxide by flue gas organic amine method | |
| CN101830813A (en) | Continuous production technique for ethoxyl ethylene diamine and reaction kettle thereof | |
| CN112266119A (en) | Bromine extraction process and device for waste water generated in production of brominated butyl rubber | |
| CN201343450Y (en) | Dedicated reactor for preparing manganese sulfate solution with leached pyrolusite from sulfur dioxide gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |