Equipment and method for producing hydrogen by decomposing hydrogen sulfide

Abstract

The invention discloses hydrogen sulfide decomposition hydrogen production equipment and method, and relates to the technical field of hydrogen sulfide treatment.The hydrogen sulfide decomposition hydrogen production equipment comprises a gas-liquid mixer, an oxidation absorption tower, a solid-liquid separator and an electrolytic bath, and the feeding end of the gas-liquid mixer is communicated with the output end of an oxidation liquid circulation line and the output end of a hydrogen sulfide-containing mixed gas conveying line; the oxidation absorption tower is provided with a first gas-liquid mixing gas inlet, a second gas-liquid mixing gas inlet and a third gas-liquid mixing gas inlet, and the angles between the axes of the discharge ends of the first gas-liquid mixing gas inlet, the second gas-liquid mixing gas inlet and the third gas-liquid mixing gas inlet and the central axis of the oxidation absorption tower are 13-15 DEG C, 15-17 DEG C and 45-47 DEG C respectively. The invention also provides a method for producing hydrogen by decomposing hydrogen sulfide. The hydrogen sulfide which is not absorbed by the absorption reactor is further converted, the adhesion of a solid phase is reduced, mixing is carried out by virtue of fluid interaction, the contact area of the gas phase and the liquid phase is increased, and the mass transfer efficiency is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrogen sulfide treatment, and in particular to a hydrogen sulfide decomposition hydrogen production device and method. Background Art

[0002] Hydrogen sulfide is a highly harmful toxic gas produced by the oil, natural gas and petrochemical industries. Most companies use the Claus process to treat it. The main purpose is to recover the sulfur in the hydrogen sulfide, and the hydrogen in it generates water through oxidation. In recent years, the country has vigorously promoted the use of hydrogen energy. How to convert the hydrogen element in hydrogen sulfide into hydrogen energy is a hot topic of research at home and abroad. Hydrogen sulfide can be decomposed by microwave method, catalytic thermal decomposition, photocatalytic decomposition and other technologies to produce hydrogen. It is currently limited to the experimental stage and basically has not been industrialized. The more mature technology of producing hydrogen from hydrogen sulfide by indirect electrochemical method has gradually matured and has been promoted. At the same time, there are also some defects. This patent is a further improvement of the production of hydrogen from hydrogen sulfide.

[0003] The indirect electrochemical method is used to decompose hydrogen sulfide to produce sulfur and hydrogen at the same time. This technology first uses gaseous hydrogen sulfide and liquid oxidant to produce solid sulfur. The reaction is carried out in an oxidation reaction vessel. The hydrogen sulfide conversion rate is 85-90%. During the reaction, gas, liquid and solid phases exist simultaneously. The oxidant is liquid, usually prepared with Fe2(SO4)3+H2SO4 solution. H2S is absorbed by Fe in the absorption reactor. 3+ The oxidizing liquid is oxidized to form sulfur particles, while Fe 3+ Also reduced to Fe 2+ The slurry containing sulfur particles is sent to the solid-liquid separator. After the sulfur is removed, the H + and Fe 2+ The solution is sent to the electrolytic reactor, and at the anode Fe 2+ Oxidized to Fe 3+ , and then sent back to the absorption reactor for recycling, H + It passes through the ion exchange membrane into the cathode and is reduced to H2, which is released from the cathode.

[0004] The reaction of the whole process is as follows:

[0005] In the absorption reactor: Fe2(SO4)3+H2S=2FeSO4+S↓+H2SO4

[0006] Ionic formula: 2Fe 3+ +H2S=2Fe 2+ +2H++S↓

[0007] Electrolytic cell reaction: FeSO4+H2SO4+=Fe2(SO4)3+H2↑

[0008] Ionic formula: 2Fe2+ +2H+=2Fe 3+ +H2↑

[0009] The total reaction of the whole process: H2S=S↓+H2↑

[0010] The process mainly consists of two parts: the absorption reactor produces elemental sulfur and the electrolyzer produces hydrogen. The main problem is that hydrogen sulfide cannot be completely converted into hydrogen and sulfur, and the conversion rate is low.

[0011] Secondly, the absorption reactor is seriously corroded and blocked. Since the oxidizing medium contains strong acid radicals and is highly corrosive, how to select materials to avoid corrosion plays an important role in this technology. For containers where gas, liquid and solid phases exist simultaneously, the internal structure is also very important. Solid sulfur particles generated during the oxidation process are easy to gather and adhere to the inlet and outlet pipes, the inner wall of the tower, the packing layer, the gas-liquid distribution plate and other tower internals, blocking the container. The oxidation process of H2S is a fast reaction process controlled by mass transfer. The design of the reactor can prevent corrosion and avoid blockage, which can improve the production capacity of the entire process.

[0012] Traditional oxidizers include packed towers, bubbling towers, stirring and mixing towers, etc. Packed towers cannot be operated because solid sulfur is easily blocked when the channel is generated; bubbling towers have a small gas-liquid mass transfer area and low mass transfer efficiency. Solid products generated during the oxidation process are easy to block the gas distributor and affect the distribution of gas. Mixed towers with stirring have strong acid radicals in the oxidizing liquid, which seriously corrodes the transmission shaft, bearings, seals and other parts. These defects make traditional absorption towers unusable for long periods of time.

[0013] The internal circulation absorption reactor disclosed in the patent publication number CN100450917C has a relatively complex internal structure and high manufacturing and maintenance costs. When the gap between the inner tube and the casing is large, the gas and liquid cannot be mixed. When the gap is small, solid sulfur may adhere to the tube wall and cause blockage. From the perspective of chemical structure, the gas phase coming out of the inner tube cannot all turn up, and a part of it comes out directly from the bottom. The resistance coming out from the bottom is smaller than the resistance turning up, and the purpose of gas-liquid mixing cannot be achieved.

[0014] The jet absorption reactor with patent publication number CN107537301B is also only suitable for laboratory use. When the reaction scale is expanded, it will have defects such as uneven mixing, airflow stringing, and reduced efficiency.

[0015] Therefore, those skilled in the art provide a hydrogen production device by decomposing hydrogen sulfide to solve the problems raised in the above background technology. Summary of the invention

[0016] The invention provides a hydrogen production device and method for decomposing hydrogen sulfide. The method improves the conversion rate of hydrogen sulfide, adds a high-temperature cracking reactor, further converts the hydrogen sulfide not absorbed by the absorption reactor, and transforms the absorption reactor to reduce the adhesion of the solid phase, avoids the sulfur blockage of the tower body and pipes, and optimizes and improves the problems of equipment corrosion, poor reaction stability and low efficiency; the method relies on the interaction of fluids for mixing, increases the contact area of ​​gas-liquid two phases, and improves the mass transfer efficiency.

[0017] In order to achieve the above object, the present invention provides the following technical solutions:

[0018] The present invention first provides a hydrogen production device by decomposing hydrogen sulfide, comprising:

[0019] A gas-liquid mixer, wherein the feed end of the gas-liquid mixer is respectively connected to the output end of the oxidation liquid circulation line and the mixed gas transmission line containing hydrogen sulfide, and the diameter of the top and bottom ends of the gas-liquid mixer is larger than the diameter of the middle part;

[0020] An oxidation absorption tower, wherein the oxidation absorption tower is provided with a first gas-liquid mixed air inlet, a second gas-liquid mixed air inlet and a third gas-liquid mixed air inlet, the first gas-liquid mixed air inlet, the second gas-liquid mixed air inlet and the third gas-liquid mixed air inlet are all arranged along the outer wall of the oxidation absorption tower, and the first gas-liquid mixed air inlet, the second gas-liquid mixed air inlet and the third gas-liquid mixed air inlet are located in the same plane, the first gas-liquid mixed air inlet, the second gas-liquid mixed air inlet and the third gas-liquid mixed air inlet are connected to the discharge end of the gas-liquid mixer through a conveying pipeline, and the angles between the discharge end axes of the first gas-liquid mixed air inlet, the second gas-liquid mixed air inlet and the third gas-liquid mixed air inlet and the central axis of the oxidation absorption tower are 13-15°C, 15-17°C and 45-47°C respectively;

[0021] A solid-liquid separator, which separates sulfur from the reaction liquid. The feed end of the solid-liquid separator is connected to the liquid phase outlet containing solid particles at the bottom of the oxidation absorption tower through a delivery pipeline. A delivery pump is provided on the delivery pipeline. The liquid containing light sulfur particles is above the liquid surface of the oxidation absorption tower. The slurry of light sulfur particles is delivered to the solid-liquid separator through the delivery pipeline.

[0022] The electrolytic cell has a feed end connected to a top discharge end of a solid-liquid separator through a delivery pipeline. The electrolytic cell receives the clear liquid delivered by the solid-liquid separator, and the electrolytic cell electrolyzes the clear liquid to produce hydrogen. The remaining oxidized liquid after electrolysis in the electrolytic cell is returned to the gas-liquid mixer through an oxidized liquid circulation line.

[0023] Furthermore, another liquid phase outlet containing solid particles of the oxidation absorption tower is connected to the feed end of the first delivery pump, and another liquid phase outlet containing solid particles is arranged above the plane where the first gas-liquid mixed air inlet, the second gas-liquid mixed air inlet and the third gas-liquid mixed air inlet are located, and the slurry containing heavier particles is transported from the liquid phase outlet containing solid particles at the lower part of the oxidation absorption tower to the solid-liquid separator.

[0024] Furthermore, a wire mesh demister is provided on the top of the oxidation absorption tower, and the wire mesh demister is located above another liquid phase outlet containing solid particles; the third discharge end of the oxidation absorption tower is connected to the gas-liquid separator through the top gas phase line, and the wire mesh demister is located below another liquid phase outlet containing solid particles; the gas after the oxidation reaction of the oxidation absorption tower passes through the wire mesh demister and is transported to the gas-liquid separator by the top gas phase line, and the wire mesh demister removes the mist carried by the gas.

[0025] Furthermore, the bottom discharge end of the gas-liquid separator is connected to another feed end of the solid-liquid separator through a conveying pipeline.

[0026] Furthermore, the other discharge end of the gas-liquid separator is connected to the first inlet, the second inlet and the third inlet respectively through the induced draft fan gas phase circulation line, the first inlet, the second inlet and the third inlet are located below the plane where the first gas-liquid mixed air inlet, the second gas-liquid mixed air inlet and the third gas-liquid mixed air inlet are located, 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 located in the same plane; the incompletely oxidized hydrogen sulfide separated by the gas-liquid separator is transported to the oxidation absorption tower through the induced draft fan gas phase circulation line for re-oxidation to ensure that the hydrogen sulfide content of the exhaust gas is ≤15-10%; bubbling is carried out in different directions through the first inlet, the second inlet and the third inlet to prevent the sulfur settled at the bottom from agglomerating into lumps and causing blockage.

[0027] Furthermore, the top discharge end of the gas-liquid separator is connected to the feed end of the high-temperature cracking furnace.

[0028] Furthermore, the discharge end of the high-temperature cracking furnace is connected to the feed end of the condenser through a conveying pipeline, and the temperature of the high-temperature cracking furnace is 1150-1200°C.

[0029] Furthermore, the condenser transports the converted liquid to the collector through a transport pipeline, and the collector separates liquid sulfur. The output end of the collector is connected to the feed end of the pressure swing absorption box through a mixed gas line.

[0030] Furthermore, the pressure-switching absorption box receives the gas transmitted from the collector, separates the waste gas and hydrogen, and the waste gas is incinerated.

[0031] The present invention also provides a method for producing hydrogen by decomposing hydrogen sulfide, comprising:

[0032] Step 1: Fe2(SO4)3 and H2SO4 solutions are prepared into oxidant A solution, and after the oxidant A solution and the mixed gas B containing H2S are mixed with each other in a gas-liquid mixer, the gas-liquid two-phase is ejected at a high speed from the necking port in the middle of the liquid mixer;

[0033] Step 2: The fluid ejected from the gas-liquid mixer at high speed enters the oxidation absorption tower in three ways in the same radial direction. The three feed inlets are at 13-15°C, 15-17°C, and 45-47°C with the center axis of the tower. In the oxidation absorption tower, Fe 3+ Reacts with H2S to generate Fe 2+ With S, H + It is released in the form of H2SO4, and single-substance particles S are formed in the liquid phase. The light sulfur single-substance particles float up with the airflow and gather at the top of the oxidation absorption tower, while the heavy sulfur single-substance sinks to the bottom of the oxidation absorption tower.

[0034] Step 3: The slurry of light sulfur particles gathered at the upper part of the oxidation absorption tower is discharged through the liquid phase outlet pipeline containing solid particles, and the slurry containing heavier particles is discharged from the liquid phase outlet pipeline containing solid particles at the lower part of the tower, and is transported to the solid-liquid separator through a delivery pump, where the solid sulfur and the reaction liquid are separated;

[0035] Step 4: After the solid sulfur is separated in the separator, the clear liquid enters the electrolytic cell. + The electrons move to the cathode and become H2, which is released into liquid Fe 2+ Losing electrons at the anode reduces to Fe 3+ It is converted into oxidation liquid and returned to the gas-liquid mixer through the oxidation liquid circulation line in the form of Fe2(SO4)3 for repeated use;

[0036] Step 5: The oxidized gas comes out from the top of the oxidation absorption tower, passes through the wire mesh demister at the top of the oxidation absorption tower, and enters the gas-liquid separator from the gas phase line at the top of the tower. The gas-liquid separator separates a large amount of liquid carried in the gas and returns to the solid-liquid separator;

[0037] Step 6: 1 / 4 to 1 / 5 of the gas from the gas-liquid separator is recycled into the oxidation absorption tower through the first inlet, the second inlet and the third inlet in three ways;

[0038] Step 7: The gas coming out of the top of the gas-liquid separator enters the high-temperature cracking furnace to decompose the unabsorbed hydrogen sulfide at high temperature to produce gaseous sulfur and hydrogen;

[0039] Step 8: After the gaseous sulfur and hydrogen generated in step 7 are cooled by a condenser, the gaseous sulfur changes into a liquid phase and enters a collector to form liquid sulfur flowing out, and the gas phase part enters a pressure swing adsorption box through a mixed gas line to perform pressure swing adsorption on the gas;

[0040] Step 9: After pressure swing adsorption, hydrogen is separated from other mixed gases and converted into pure hydrogen. Other gases are burned in the incinerator and then discharged after being treated with alkaline solution.

[0041] In the above technical solution, the present invention provides a hydrogen sulfide decomposition hydrogen production device and method, which has the following beneficial effects:

[0042] 1. Improve the conversion rate of hydrogen sulfide, add high-temperature cracking reactors, further convert the unabsorbed hydrogen sulfide, and improve the process of hydrogen production by decomposing hydrogen sulfide.

[0043] 2. Reduce the adhesion of the solid phase and avoid sulfur blockage in the tower body and pipes of the oxidation absorption tower to optimize and improve problems such as equipment corrosion, poor reaction stability and low efficiency.

[0044] 3. Relying on the external power of gas and liquid, the reaction energy is transferred through three mixing steps. First, the gas and liquid are mixed in a gas-liquid mixer outside the tower. Secondly, the oxidation absorption tower has three inward-retracted feed ports, which form a certain angle with each other. The three fluid jets collide and interact with each other to achieve the effect of oxidation reaction. Finally, the gas returning to the tower from the gas-liquid separator also interacts with each other during the rising process. The gas is dispersed into small bubbles and reacts with the liquid as it goes up, which increases the gas-liquid contact area and improves the oxidation efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0045] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments recorded in the present invention. For ordinary technicians in this field, other drawings can also be obtained based on these drawings.

[0046] Figure 1 A schematic diagram of the structure of a hydrogen sulfide decomposition hydrogen production device provided in an embodiment of the present invention;

[0047] Figure 2 for Figure 1 A cross-sectional view of the first gas-liquid mixing inlet on the middle oxidation absorption tower;

[0048] Figure 3 for Figure 1 A cross-sectional view of the first inlet portion of the intermediate oxidation absorption tower.

[0049] In the figure:

[0050] 1. Gas-liquid mixer; 2. Oxidation absorption tower; 3. Solid-liquid separator; 4. Electrolyzer; 5. High-temperature cracking furnace; 6. Condenser; 7. Collector; 8. Voltage transformer absorption box; 9. Gas-liquid separator;

[0051] 101. Oxidation liquid circulation line; 102. Mixed gas transmission line;

[0052] 201, first gas-liquid mixed air inlet; 202, second gas-liquid mixed air inlet; 203, third gas-liquid mixed air inlet; 204, liquid phase outlet containing solid particles; 205, liquid phase outlet containing solid particles; 206, wire mesh demister; 207, tower top gas phase line; 208, first inlet; 209, second inlet; 210, third inlet;

[0053] 301, delivery pump;

[0054] 401. induced draft fan gas phase circulation line;

[0055] 701. Mixed gas line. DETAILED DESCRIPTION

[0056] In order to enable those skilled in the art to better understand the technical solution of the present invention, the present invention will be further described in detail below with reference to the accompanying drawings.

[0057] See also Figure 1 -3;

[0058] A hydrogen production device for decomposing hydrogen sulfide according to an embodiment of the present invention comprises:

[0059] A gas-liquid mixer 1, wherein the feed end of the gas-liquid mixer 1 is respectively connected to the output ends of the oxidation liquid circulation line 101 and the mixed gas delivery line 102 containing hydrogen sulfide, and the diameters of the top and bottom ends of the gas-liquid mixer 1 are larger than the diameter of the middle part;

[0060] The oxidation absorption tower 2 is provided with a first gas-liquid mixed air inlet 201, a second gas-liquid mixed air inlet 202 and a third gas-liquid mixed air inlet 203, the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 are all arranged along the outer wall of the oxidation absorption tower 2, and the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 are located in the same plane, The first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 are connected to the discharge end of the gas-liquid mixer 1 through a conveying pipeline, and the angles between the discharge end axes of the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 and the central axis of the oxidation absorption tower 2 are 13-15°C, 15-17°C, 45-47°C, preferably 14°C, 16°C, 46°C;

[0061] A solid-liquid separator 3, wherein the solid-liquid separator 3 separates sulfur from the reaction liquid. The feed end of the solid-liquid separator 3 is connected to the liquid phase outlet 204 containing solid particles at the bottom of the oxidation absorption tower 2 through a delivery pipeline. A delivery pump 301 is provided on the delivery pipeline. The liquid containing light sulfur particles is above the liquid surface of the oxidation absorption tower 2. The slurry of light sulfur particles is delivered to the solid-liquid separator 3 through the delivery pipeline.

[0062] The electrolytic cell 4 has a feed end connected to the top discharge end of the solid-liquid separator 3 via a delivery pipeline. The electrolytic cell 4 receives the clear liquid delivered by the solid-liquid separator 3, and the electrolytic cell 4 electrolyzes the clear liquid to produce hydrogen. The remaining oxidizing liquid after electrolysis in the electrolytic cell 4 is returned to the gas-liquid mixer 1 via the oxidizing liquid circulation line 101.

[0063] Another liquid phase outlet 205 containing solid particles of the oxidation absorption tower 2 is connected to the feed end of the first delivery pump 206, and another liquid phase outlet 205 containing solid particles is arranged above the plane where the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 are located. The slurry containing heavier particles is transported from the liquid phase outlet 205 containing solid particles at the lower part of the oxidation absorption tower 2 to the solid-liquid separator 3. A wire mesh demister 206 is provided on the top of the oxidation absorption tower 2, and the wire mesh demister 206 is located above another liquid phase outlet 205 containing solid particles; the third discharge end of the oxidation absorption tower 2 is connected to the gas-liquid separator 9 through the top gas phase line 207, and the wire mesh demister 206 is located below another liquid phase outlet 205 containing solid particles; the gas after the oxidation reaction of the oxidation absorption tower 2 passes through the wire mesh demister 206 and is transported to the gas-liquid separator 9 by the top gas phase line 207, and the wire mesh demister 206 removes the mist carried by the gas.

[0064] The bottom discharge end of the gas-liquid separator 9 is connected to the other feed end of the high-temperature cracking furnace 5 through a conveying pipeline. The other discharge end of the gas-liquid separator 9 is connected to the first inlet 208, the second inlet 209 and the third inlet 210 respectively through the induced draft fan gas phase circulation line 401, the first inlet 208, the second inlet 209 and the third inlet 210 are located below the plane where the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 are located, the first inlet 208, the second inlet 209 and the third inlet 210 are 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 located in the same plane; the incompletely oxidized hydrogen sulfide separated by the gas-liquid separator 9 is transported to the oxidation absorption tower 2 for re-oxidation through the induced draft fan gas phase circulation line 401 to ensure that the hydrogen sulfide content of the exhaust gas is ≤15-10%; bubbling in different directions through the first inlet, the second inlet and the third inlet is prevented from agglomerating into blocks and causing blockage.

[0065] The top discharge end of the gas-liquid separator 9 is connected to the feed end of the high-temperature cracking furnace 5. The discharge end of the high-temperature cracking furnace 5 is connected to the feed end of the condenser 6 through a conveying pipeline, and the temperature of the high-temperature cracking furnace 5 is 1150-1200°C. The condenser 6 transports the converted liquid to the collector 7 through a conveying pipeline, and the collector 7 separates liquid sulfur. The output end of the collector 7 is connected to the feed end of the pressure-switching absorption box 8 through a mixed gas line 701. The pressure-switching absorption box 8 receives the gas transmitted from the collector 7, and separates the waste gas and hydrogen, and the waste gas is incinerated.

[0066] The present invention also provides a method for producing hydrogen by decomposing hydrogen sulfide, the specific process is as follows (see attached Figure 1 ):

[0067] The first step is to prepare an oxidant A solution with Fe2(SO4)3 and H2SO4 solution in a molar ratio of 4:1, and mix it with a mixed gas B containing H2S through a gas-liquid mixer 1, wherein the molar ratio of the oxidant A solution to the mixed gas B is preferably 5-10:1; the mixed gas containing H2S generally comes from refinery acid gas and oil and gas field natural gas, and the concentration of H2S in the mixed gas B is preferably 0.5% to 80%. The gas-liquid mixer 1 has a diameter at both ends and a small diameter in the middle. When the gas-liquid fluid changes from a large-diameter trumpet-shaped channel to a small-diameter channel, the flow rate will increase sharply, and the gas-liquid two-phase will be ejected at a high speed from the necking port in the middle of the gas-liquid mixer 1;

[0068] In the second step, the fluid ejected at high speed from the gas-liquid mixer 1 enters the oxidation absorption tower 2 in three ways in the same radial direction through the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203. The axes of the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 are 13-15°C, 15-17°C and 45-47°C with the central axis of the oxidation absorption tower 2, respectively, preferably 14°C, 16°C and 46°C, so that the liquid phase ejected from the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 is in a triangular shape, and the three gas-liquid streams collide with each other and interact with each other (see Figure 2 As shown), the oxidation reaction liquid is driven to rotate clockwise, Fe 3+ Reacts with H2S to generate Fe 2+ With S, H + It is released in the form of H2SO4. The better the gas-liquid mixing, the faster the reaction. Elemental particles S are formed in the liquid phase. The light sulfur elemental particles float up with the airflow and gather at the upper part of the tower. The heavy sulfur elemental particles sink to the bottom of the oxidation absorption tower 2.

[0069] Step 3: The slurry of light sulfur particles gathered in the upper part of the oxidation absorption tower 2 is discharged through the liquid phase outlet 205 pipeline containing solid particles, and the slurry containing heavier particles is discharged from the lower part of the tower through the liquid phase outlet 204 pipeline containing solid particles, and is transported to the solid-liquid separator 3 through the delivery pump 301. In the solid-liquid separator 3, the solid sulfur is separated from the reaction liquid by precipitation, centrifugal separation and other measures;

[0070] Step 4: After the solid sulfur is separated in the solid-liquid separator 3, the clear liquid enters the electrolytic cell 4, where H + The electrons move to the cathode and become H2, which is released into liquid Fe 2+ Losing electrons at the anode reduces to Fe 3+ It is converted into an oxidizing liquid and returned to the gas-liquid mixer 1 in the form of Fe2(SO4)3 through the oxidizing liquid circulation line 101 for repeated use;

[0071] Step 5: The oxidized gas comes out from the top of the oxidation absorption tower 2, and the hydrogen sulfide conversion rate is 85-90%. The gas after the oxidation reaction passes through the wire mesh demister 206 at the top of the tower and enters the gas-liquid separator 9 from the top gas phase line 207. The wire mesh demister 206 mainly removes the mist carried by the gas. The gas-liquid separator 9 separates a large amount of liquid carried in the gas and returns to the solid-liquid separator 3.

[0072] Step 6: 1 / 4 to 1 / 5 of the gas from the gas-liquid separator 9 is recycled through the induced draft fan gas phase circulation line 401 in three ways through the first inlet 208, the second inlet 209 and the third inlet 210 into the oxidation absorption tower 2 for recirculation. First, the insufficiently oxidized hydrogen sulfide is oxidized again to ensure that the hydrogen sulfide content of the exhaust gas is ≤15-10%; second, the three air inlet pipes are bubbled in different directions to prevent the sulfur settled at the bottom from agglomerating into blocks and causing blockage.

[0073] Step 7: The gas from the top of the gas-liquid separator 9 enters the high-temperature cracking furnace 5, the temperature is preferably 1150-1200°C, and the furnace is oxygen-free to prevent S oxidation. The hydrogen sulfide not absorbed in the equipment is subjected to high-temperature decomposition to produce gaseous sulfur and hydrogen, the purpose of which is to improve the conversion rate of hydrogen sulfide. The high-temperature cracking furnace 5 is suitable for the condition of low hydrogen sulfide concentration, generally the hydrogen sulfide content is ≤5%, the low hydrogen sulfide concentration reacts thoroughly, and the conversion rate is high;

[0074] Step 8: After the gaseous sulfur and hydrogen are cooled by the condenser 6, the gaseous sulfur changes into liquid phase and enters the collector 7 to form liquid sulfur flowing out. The gas phase part enters the pressure swing adsorption box 8 through the mixed gas line 701. The pressure swing adsorption box 8 contains adsorbent. The adsorbent has different adsorption amount, adsorption speed and adsorption force for different gases. The pressure swing adsorption selects different adsorbents according to the characteristics of hydrogen to achieve hydrogen separation.

[0075] The ninth step is to separate hydrogen from other mixed gases through pressure swing adsorption and turn it into pure hydrogen. Other gases are burned in the incinerator and then discharged after being treated with alkali solution. The mixed gas containing H2S generally comes from oil and gas fields and petrochemical industries and contains N2, CO, CO2, O2 and some organic sulfur, which need to be burned.

[0076] In the above process, hydrogen sulfide reacts twice. The first time is oxidation by strong acid. 2－ In the device of the present application, sulfur is oxidized into elemental sulfur, H + It is reduced to H2 in the electrolytic cell 4. In this reaction process, 10-15% of the H2S in the mixed gas does not react. The remaining H2S enters the cracking furnace and belongs to the second reaction, which is directly decomposed at high temperature: H2S=S+H2. The hydrogen sulfide content in the final exhaust gas is ≤0.5-0.1%. The high-temperature cracking and decomposition reaction has harsh reaction conditions and reverse reactions. It needs to be condensed quickly and is suitable for the decomposition of low-concentration hydrogen sulfide.

[0077] In the first reaction process, the oxidation absorption tower 2 is an important equipment. Since the oxidation liquid is Fe2(SO4)3+H2SO4 solution or FeCI3+HCI solution, both are highly corrosive, the equipment is lined with graphite polytetrafluoroethylene material, lead enamel or enamel. The applicable temperature is 0~+150℃, and the equipment can withstand 500~800Kpa.

[0078] The filler in the wire mesh demister 206 is made of acid-resistant phenolic plastic, polyethylene or other non-metallic materials. The first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet are on the same horizontal plane, and the center line of the tube is at different angles to the axis of the oxidation absorption tower 2. The first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet are retracted, and the liquid comes out in a jet shape and is in a regular triangle state inside. The gas and liquid in each path collide with each other, and the bubbles become thinner and smaller, fully integrated into the liquid, and the liquid phase in the oxidation absorption tower 2 is driven to rotate slowly in the clockwise direction. During the process of hydrogen sulfide rotating and rising from the bottom of the oxidation absorption tower 2, it is fully converted into sulfur.

[0079] 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 spray bubbles in radial and circumferential directions respectively. After interaction, the bubbles float up from the bottom of the tower and return to the oxidation absorption tower 2 to be fully oxidized.

[0080] The entire oxidation absorption tower 2 has basically no accessories inside, in order to prevent the elemental sulfur particles from being adsorbed and blocked, and also to facilitate the implementation of anti-corrosion.

[0081] The gas-liquid mixer 1 of the oxidation absorption tower 2 is a container with bell-shaped ends and a constricted interior, and a spiral guide plate is provided in the bell-shaped outlet end, so that the gas and liquid rotate at high speed after coming out.

[0082] The present invention is further described in detail below with reference to specific embodiments.

[0083] Example 1

[0084] A certain oil and gas field uses a mixed gas containing 30% hydrogen sulfide, and the remaining gases are N2, CO, CO2, etc., which is used with Fe-rich 3+ Fe2(SO4)3+H2SO4 solution (the molar ratio of Fe2(SO4)3 and H2SO4 solution is 4:1) is used as oxidant, and the adsorption reaction temperature is 80℃.

[0085] The gas and liquid enter the gas-liquid mixer 1 at a molar ratio of 1:8. After the gas and liquid are mixed, they enter the oxidation absorption tower 2 through the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 at a speed of 1.5 m / s in three ways. The axes of the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 are 14°C, 16°C and 46°C with the central axis of the oxidation absorption tower 2 respectively. The pipe outlet is retracted, and the liquid comes out in a jet shape. It is in a regular triangle shape when viewed from the inside. The gas and liquid in each way collide with each other, and the bubbles become thinner and smaller, fully integrated into the liquid, and the slurry phase in the tower is driven to rotate slowly in the clockwise direction. During the rising process of the mixed gas, S in hydrogen sulfide 2－Oxidized to elemental sulfur, Fe 3+ Reduced to Fe 2+ The light sulfur particles float up with the air flow and gather at the top of the oxidation absorption tower, while the heavy sulfur particles sink to the bottom of the oxidation absorption tower.

[0086] The slurry of light sulfur particles gathered in the upper part of the oxidation absorption tower 2 is discharged through the liquid phase outlet 205 pipeline containing solid particles, and the slurry containing heavier particles is discharged from the liquid phase outlet 204 pipeline containing solid particles in the lower part of the tower, and is transported to the solid-liquid separator 3 through the delivery pump 301, and the solid sulfur and the reaction liquid are separated in the solid-liquid separator 3;

[0087] After the solid sulfur is separated in the separator 3, the clear liquid enters the electrolytic cell 4, where H + The electrons move to the cathode and become H2, which is released into liquid Fe 2+ Losing electrons at the anode reduces to Fe 3+ It is converted into an oxidizing liquid and returned to the gas-liquid mixer 1 in the form of Fe2(SO4)3 through the oxidizing liquid circulation line 101 for repeated use;

[0088] The residual gas after the oxidation reaction contains 3% hydrogen sulfide, and comes out from the top of the oxidation absorption tower 2, passes through the wire mesh demister 206 at the top of the oxidation absorption tower 2, and enters the gas-liquid separator 9 through the top gas phase line 207. The gas-liquid separator 9 separates a large amount of liquid carried in the gas and returns to the solid-liquid separator 3;

[0089] The gas 1 / 4 induced draft fan gas phase circulation line 401 from the gas-liquid separator 9 is divided into three paths and enters the oxidation absorption tower 2 for recycling through the first inlet 208, the second inlet 209 and the third inlet 210;

[0090] 3 / 4 of the gas from the gas-liquid separator 9 enters the high-temperature cracking furnace. The gas entering the high-temperature cracking furnace is a mixed gas containing N2, CO, CO2, H2S, etc. Hydrogen sulfide is cracked at high temperature and condensed rapidly. After cracking, the gaseous sulfur is condensed into liquid sulfur and hydrogen. After cooling by the condenser 6, the gaseous sulfur becomes liquid and enters the collector 7 to form liquid sulfur outflow. The mixed gas is adsorbed by the pressure swing adsorption box 8 to produce pure hydrogen. The rest enters the incinerator for combustion and then enters the alkali liquid absorber for emptying. The total conversion rate of hydrogen sulfide is 99.5-99.7%.

[0091] Example 2

[0092] A chemical plant uses a mixed gas containing 45% to 50% hydrogen sulfide, and the remaining gases are N2, CO, CO2, COS, etc., to react with Fe-rich 3+ Fe2(SO4)3+H2SO4 solution (wherein the molar ratio of Fe2(SO4)3 and H2SO4 solution is 4:1) is used as oxidant. The oxidation absorption tower has a diameter of 800mm and a height of 12000mm. The interior is lead-lined and the adsorption reaction temperature is 70-80℃.

[0093] The gas and liquid enter the gas-liquid mixer 1 at a molar ratio of 1:10. After the gas and liquid are mixed, they enter the oxidation absorption tower 2 through the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 at a speed of 1.8 m / s in three ways. The axes of the first gas-liquid mixed air inlet 201, the second gas-liquid mixed air inlet 202 and the third gas-liquid mixed air inlet 203 are 14°C, 16°C and 46°C with the central axis of the oxidation absorption tower 2 respectively. The pipe outlet is retracted, and the liquid comes out in a jet shape. It is in a regular triangle shape when viewed from the inside. The gas and liquid in each way collide with each other, and the bubbles become thinner and smaller, fully integrated into the liquid, and the slurry phase in the tower is driven to rotate slowly in the clockwise direction. During the rising process of the mixed gas, S in hydrogen sulfide 2－ Oxidized to elemental sulfur, Fe 3+ Reduced to Fe 2+ The light sulfur particles float up with the air flow and gather at the top of the oxidation absorption tower, while the heavy sulfur particles sink to the bottom of the oxidation absorption tower.

[0094] The slurry of light sulfur particles gathered in the upper part of the oxidation absorption tower 2 is discharged through the liquid phase outlet 205 pipeline containing solid particles, and the slurry containing heavier particles is discharged from the liquid phase outlet 204 pipeline containing solid particles in the lower part of the tower, and is transported to the solid-liquid separator 3 through the delivery pump 301, and the solid sulfur and the reaction liquid are separated in the solid-liquid separator 3;

[0095] After the solid sulfur is separated in the separator 3, the clear liquid enters the electrolytic cell 4, where H + The electrons move to the cathode and become H2, which is released into liquid Fe 2+ Losing electrons at the anode reduces to Fe 3+ It is converted into an oxidizing liquid and returned to the gas-liquid mixer 1 in the form of Fe2(SO4)3 through the oxidizing liquid circulation line 101 for repeated use;

[0096] The oxidized gas comes out from the top of the oxidation absorption tower 2, and the hydrogen sulfide conversion rate is 93%. The gas after the oxidation reaction passes through the wire mesh demister 206 at the top of the tower and enters the gas-liquid separator 9 from the top gas phase line 207. The wire mesh demister 206 mainly removes the mist carried by the gas. The gas-liquid separator 9 separates a large amount of liquid carried in the gas and returns to the solid-liquid separator 3;

[0097] The gas 1 / 5 of the induced draft fan gas phase circulation line 401 from the gas-liquid separator 9 is divided into three paths and enters the oxidation absorption tower 2 for recycling through the first inlet 208, the second inlet 209 and the third inlet 210;

[0098] 4 / 5 of the gas from the gas-liquid separator 9 enters the high-temperature cracking furnace, hydrogen sulfide is cracked at high temperature and condensed quickly, and the gaseous sulfur after cracking is condensed into liquid sulfur and hydrogen. The hydrogen sulfide content of the gas after the high-temperature cracking reaction is 0.4%. After cooling by the condenser 6, the gaseous sulfur becomes liquid and enters the collector 7 to form liquid sulfur outflow. The mixed gas is adsorbed by the pressure swing adsorption box 8 to produce pure hydrogen. The rest enters the incinerator for combustion and then enters the alkali liquid absorber for emptying. The total conversion rate of hydrogen sulfide is 99.1% to 99.2%.

[0099] Compared with Example 1, the concentration of hydrogen sulfide in this example increases, the reaction rate increases, and the conversion rate decreases.

[0100] Due to the simple internal structure and proper anti-corrosion measures, there is no blockage or corrosion during the operation of the oxidation absorption tower.

[0101] Example 3

[0102] The reaction steps and conditions are the same as those in Example 1, except that a mixed gas containing 5-80% hydrogen sulfide and the rest CO2, CO, N2, etc. is used to react with Fe-rich 3+ Fe2(SO4)3+H2SO4 solution (wherein the molar ratio of Fe2(SO4)3 and H2SO4 solution is 4:1) is mixed by gas-liquid, the gas-liquid molar ratio is 1:5-10, and the temperature in the tower is 80°C. The specific reaction conditions and conversion rate are shown in Table 1:

[0103] Table 1

[0104]

[0105]

[0106] The experimental results in Table 1 show that the conversion rate of low-concentration hydrogen sulfide is high, the conversion rate of 1-40% hydrogen sulfide is above 99.8%, and the conversion rate of high-concentration hydrogen sulfide is low. There are many factors that affect the conversion rate, and the ratio of the oxidizing liquid, the gas circulation volume, the structure of the tower, the high-temperature cracking furnace, etc. are all very important.

[0107] Example 4

[0108] The reaction steps and conditions are the same as those in Example 1, except that a mixed gas containing 15% hydrogen sulfide and the rest CO2, COS, N2, etc. is used to react with Fe-rich 3+ The Fe2(SO4)3+H2SO4 solution (wherein the molar ratio of Fe2(SO4)3 and H2SO4 solution is 4:1) is mixed by gas-liquid mixing, and the gas-liquid molar ratio is 1:10.

[0109] In Example 4, the hydrogen sulfide conversion rate was 99.8%.

[0110] Compared with the prior art, the present invention adds a step of the residual gas entering the high-temperature cracking furnace, thereby improving the conversion rate of hydrogen sulfide. The improved oxidation absorption tower has no tower internals. During use, the gas and liquid are mixed three times. First, they are mixed in the gas-liquid mixer outside the tower; second, there are three jet ports entering the oxidation absorption tower, and the liquid comes out in a regular triangle state inside, and the three air flows interact with each other. Third, the three residual gases coming out of the gas-liquid separator return and are ejected from the bottom of the tower. They also interact with each other during the rising process, and the gas is dispersed into fine bubbles while reacting with the liquid going up. These increase the gas-liquid contact area, thereby effectively improving the oxidation efficiency.

[0111] The above description is only by way of illustration of certain exemplary embodiments of the present invention. It is undoubted that those skilled in the art can modify the described embodiments in various ways without departing from the spirit and scope of the present invention. Therefore, the above drawings and descriptions are illustrative in nature and should not be construed as limiting the scope of protection of the claims of the present invention.

Claims

1. A hydrogen production equipment by decomposing hydrogen sulfide, characterized in that: include: A gas-liquid mixer (1), wherein the feed end of the gas-liquid mixer (1) is respectively connected to the output ends of the oxidation liquid circulation line (101) and the mixed gas delivery line (102) containing hydrogen sulfide, and the diameters of the top and bottom ends of the gas-liquid mixer (1) are larger than the diameter of the middle part; An oxidation absorption tower (2), wherein the oxidation absorption tower (2) is provided with a first gas-liquid mixed air inlet (201), a second gas-liquid mixed air inlet (202) and a third gas-liquid mixed air inlet (203), wherein the first gas-liquid mixed air inlet (201), the second gas-liquid mixed air inlet (202) and the third gas-liquid mixed air inlet (203) are all provided along the outer wall of the oxidation absorption tower (2), and the first gas-liquid mixed air inlet (201), the second gas-liquid mixed air inlet (202) and the third gas-liquid mixed air inlet (203) are 203) are located in the same plane, the first gas-liquid mixed air inlet (201), the second gas-liquid mixed air inlet (202) and the third gas-liquid mixed air inlet (203) are connected to the discharge end of the gas-liquid mixer (1) through a conveying pipeline, and the angles between the discharge end axes of the first gas-liquid mixed air inlet (201), the second gas-liquid mixed air inlet (202) and the third gas-liquid mixed air inlet (203) and the central axis of the oxidation absorption tower (2) are 13-15°, 15-17° and 45-47° respectively; A solid-liquid separator (3), wherein the solid-liquid separator (3) separates sulfur from the reaction liquid. The feed end of the solid-liquid separator (3) is connected to a liquid phase outlet (204) containing solid particles at the bottom of the oxidation absorption tower (2) through a delivery pipeline. A delivery pump (301) is provided on the delivery pipeline. The liquid containing light sulfur particles is above the liquid surface of the oxidation absorption tower (2). The slurry of light sulfur particles is delivered to the solid-liquid separator (3) through the delivery pipeline. An electrolytic cell (9), wherein the feed end of the electrolytic cell (9) is connected to the top discharge end of the solid-liquid separator (3) via a conveying pipeline, the electrolytic cell (9) receives the clear liquid conveyed by the solid-liquid separator (3), the electrolytic cell (9) electrolyzes the clear liquid to produce hydrogen, and the remaining oxidizing liquid after electrolysis in the electrolytic cell (9) is returned to the gas-liquid mixer (1) via the oxidizing liquid circulation line (101).

2. A hydrogen production equipment by decomposing hydrogen sulfide according to claim 1, characterized in that: Another liquid phase outlet (205) containing solid particles of the oxidation absorption tower (2) is connected to the feed end of the first delivery pump (206), and another liquid phase outlet (205) containing solid particles is arranged above the plane where the first gas-liquid mixed air inlet (201), the second gas-liquid mixed air inlet (202) and the third gas-liquid mixed air inlet (203) are located. The slurry containing heavier particles is transported from the liquid phase outlet (205) containing solid particles at the lower part of the oxidation absorption tower (2) to the solid-liquid separator (3).

3. A hydrogen production equipment by decomposing hydrogen sulfide according to claim 1, characterized in that: A wire mesh demister (206) is provided at the top of the oxidation absorption tower (2), and the wire mesh demister (206) is located above another liquid phase outlet (205) containing solid particles; the third discharge end of the oxidation absorption tower (2) is connected to the gas-liquid separator (9) through a tower top gas phase line (207), and the wire mesh demister (206) is located below another liquid phase outlet (205) containing solid particles.

4. The hydrogen production equipment by decomposing hydrogen sulfide according to claim 1, characterized in that: The bottom discharge end of the gas-liquid separator (9) is connected to the other feed end of the high-temperature cracking furnace (5) through a conveying pipeline.

5. A hydrogen production equipment by decomposing hydrogen sulfide according to claim 4, characterized in that: The other discharge end of the gas-liquid separator (9) is connected to the first inlet (208), the second inlet (209) and the third inlet (210) respectively through the induced draft fan gas phase circulation line (401); the first inlet (208), the second inlet (209) and the third inlet (210) are located below the plane where the first gas-liquid mixed air inlet (201), the second gas-liquid mixed air inlet (202) and the third gas-liquid mixed air inlet (203) are located; 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 located in the same plane.

6. A hydrogen production equipment by decomposing hydrogen sulfide according to claim 5, characterized in that: The top discharge end of the gas-liquid separator (9) is in communication with the feed end of the high-temperature cracking furnace (5).

7. A hydrogen production equipment by decomposing hydrogen sulfide according to claim 6, characterized in that: The discharge end of the high-temperature cracking furnace (5) is connected to the feed end of the condenser (6) through a conveying pipeline, and the temperature of the high-temperature cracking furnace (5) is 1150-1200°C.

8. The hydrogen production equipment by decomposing hydrogen sulfide according to claim 7, characterized in that: The condenser (6) transports the converted liquid to the collector (7) through a transport pipeline, and the collector (7) separates liquid sulfur. The output end of the collector (7) is connected to the feed end of the pressure swing absorption box (8) through a mixed gas line (701).

9. A hydrogen production equipment by decomposing hydrogen sulfide according to claim 8, characterized in that: The pressure-switching absorption box (8) receives the gas transmitted from the collector (7), separates the waste gas and hydrogen, and the waste gas is incinerated.

10. A method for producing hydrogen by decomposing hydrogen sulfide using the device according to claim 1, characterized in that: include: Step 1: Fe2(SO4)3 and H2SO4 solutions are prepared into an oxidant A solution, and the oxidant A solution and a mixed gas B containing H2S are mixed with each other through a gas-liquid mixer (1), and the gas and liquid phases are ejected at high speed from the neck opening in the middle of the liquid mixer (1); Step 2: The fluid ejected at high speed from the gas-liquid mixer (1) enters the oxidation absorption tower (2) in three ways in the same radial direction. The three feed inlets are at 13-15°C, 15-17°C, and 45-47°C with respect to the center axis of the tower. In the oxidation absorption tower (2), Fe 3+ Reacts with H2S to generate Fe 2+ With S, H + The sulfur is released in the form of H2SO4, and elemental particles S are formed in the liquid phase. The light sulfur elemental particles float up with the air flow and gather at the upper part of the oxidation absorption tower (2), while the heavy sulfur elemental particles sink to the bottom of the oxidation absorption tower (2); Step 3: The slurry of light sulfur particles gathered at the upper part of the oxidation absorption tower (2) is discharged through the liquid phase outlet (205) pipeline containing solid particles, and the slurry containing heavier particles is discharged from the liquid phase outlet (204) pipeline containing solid particles at the lower part of the tower, and is transported to the solid-liquid separator (3) through the delivery pump (301), and the solid sulfur and the reaction liquid are separated in the solid-liquid separator (3); Step 4: After the solid sulfur is separated in the separator (3), the clear liquid enters the electrolytic cell (4), where H + The electrons move to the cathode and become H2, which is released into liquid Fe 2+ Losing electrons at the anode reduces to Fe 3+ Converted into oxidation liquid, and returned to the gas-liquid mixer (1) in the form of Fe2(SO4)3 through the oxidation liquid circulation line (101) for repeated use; Step 5: The oxidized gas is discharged from the top of the oxidation absorption tower (2), passes through the wire mesh demister (206) at the top of the oxidation absorption tower (2), and enters the gas-liquid separator (9) from the top gas phase line (207). The gas-liquid separator (9) separates a large amount of liquid carried in the gas and returns to the solid-liquid separator (3); Step 6: 1 / 4 to 1 / 5 of the gas from the gas-liquid separator (9) is recycled through the induced draft fan gas phase circulation line (401) and is divided into three paths through the first inlet (208), the second inlet (209) and the third inlet (210) into the oxidation absorption tower (2); Step 7: The gas coming out of the top of the gas-liquid separator (9) enters the high-temperature cracking furnace (5) to decompose the unabsorbed hydrogen sulfide at high temperature to produce gaseous sulfur and hydrogen; Step 8: After the gaseous sulfur and hydrogen generated in step 7 are cooled by the condenser (6), the gaseous sulfur changes into liquid phase and enters the collector (7) to form liquid sulfur flowing out, and the gas phase part enters the pressure swing adsorption box (8) through the mixed gas line (701) to perform pressure swing adsorption on the gas; Step 9: After pressure swing adsorption, hydrogen is separated from other mixed gases and converted into pure hydrogen. Other gases are burned in the incinerator and then discharged after being treated with alkali liquid.

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