Method and device for desulfurizing and decarbonizing synthesis gas

Abstract

The invention relates to a method and a device, in particular to a method and a device for desulfurizing and decarbonizing synthesis gas. The device is composed of a dust removal mechanism, an absorption mechanism and a regeneration mechanism, the dust removal mechanism comprises a rotary spraying dust removal tower, the absorption mechanism comprises a rotary spraying absorption tower, and the regeneration mechanism comprises a rotary spraying regeneration tower; the rotary spraying dust removal tower, the rotary spraying absorption tower and the rotary spraying regeneration tower are respectively composed of a tower body and a rotary spraying device. According to the device and the method, the phase boundary area of liquid can be greatly increased, the absorption can be effectively improved, and the mass transfer efficiency is improved; meanwhile, the turbulence degree of a gas phase and a liquid phase is improved, the gas-liquid contact time is prolonged, and the mass transfer efficiency is further improved. The rotary spraying device not only can replace conventional tower plates and fillers, but also can be flexibly applied to new construction of related enterprise devices and reconstruction projects of old devices; and compared with a rotary packed tower, the process is simple, the energy consumption is reduced, and the method is suitable for new equipment construction. The problem of low mass transfer efficiency in the existing desulfurization and decarbonization method is solved.

Description

Technical Field

[0001] The present invention relates to a method and a device, and particularly to a method and a device for desulfurizing and decarbonizing syngas. Background Art

[0002] As an important carrier for realizing the green and low-carbon transformation, hydrogen energy provides an effective solution for zero carbon emissions of energy. According to different raw materials, hydrogen production technologies are mainly divided into three categories: gray hydrogen (synthetic natural gas, i.e., syngas) based on fossil fuels such as coal and natural gas, hydrogen production from industrial by-products, and hydrogen production by electrolyzing water. At present, China's coal resources are relatively rich. However, due to the limitations of hydrogen production technologies, China mainly relies on fossil fuels at the present stage, and generates carbon monoxide (CO) and hydrogen through the gasification or reforming process of water and coal. This hydrogen production process accounts for about 64% of the total hydrogen production. The proportions of hydrogen production from industrial by-products and hydrogen production by electrolyzing water are about 32% and 4% respectively. Although the energy conversion efficiency of fossil fuel hydrogen production is as high as 80%, the average carbon dioxide (CO 2 )emission during its hydrogen production process is close to 14 kg / kg (calculated based on CO 2 / H 2 ), and the carbon dioxide emission is high. Its improvement plan is to effectively reduce carbon emissions by adding a carbon capture and storage (CCS) link.

[0003] At present, the most mature and widely applied carbon dioxide capture technology is the "monoethanolamine (MEA) chemical absorption method" developed in the United States. The device investment cost of this method is as high as 2000 to 3000 yuan per kilowatt, and the energy consumption required for absorbent regeneration is about 3.0 GJ / t (calculated based on CO 2 ), accounting for 60% to 70% of the operating energy consumption, and its operating cost is as high as 200 to 400 yuan / tCO 2 . Therefore, in the process of water-gas shift hydrogen production, efficiently removing CO 2 becomes a key link to improve the purity of hydrogen and reduce energy consumption.

[0004] Related patents such as 201520751715.0 and 202010842134.3 optimized the CO 2 capture and regeneration system, which is applicable to the decarbonization of high-acid natural gas or syngas with an acid gas content of up to 35%, and can make the carbon content in the purified gas lower than 2.5%. In these patents, the absorber adopts a traditional packing structure, and the mass transfer efficiency is low, resulting in low production efficiency. 202111280468.7 optimized the carbon capture system, divided the semi-lean solution into two paths, which were respectively used for regeneration and pre-absorption, so as to realize the recycling of amine liquid and reduce the energy consumption. However, these technologies still have not broken through the mass transfer limitation of the absorption device. 202111169736.8 realized synchronous desulfurization and decarbonization, and utilized liquid CO 2Evaporation and desorption are used as a cold source to cool each step in the syngas decarbonization process, saving cooling energy. Although the above patents have made innovations or optimizations in the syngas decarbonization system, a traditional packed tower is still used as the absorption tower, which not only increases the investment cost but also has low mass transfer efficiency.

[0005] From the perspective of mass transfer, increasing the turbulence degree of the flow field and improving the dispersion degree of the liquid phase are both beneficial to increasing the mass transfer area and improving the mass transfer efficiency. The plate column extends the contact time by increasing the number of plates to strengthen the mass transfer process. However, the increase in mass transfer efficiency is limited, the device volume will also increase accordingly, and the liquid phase dispersion and the turbulence degree of the flow field are low, making it difficult to achieve a breakthrough in the order of magnitude of mass transfer efficiency. Similar problems also exist in the packed tower. Therefore, it is necessary to design a method and device for desulfurization and decarbonization of syngas to solve the above problems. Summary of the Invention

[0006] The object of the present invention is to provide a method and device for desulfurization and decarbonization of syngas that can effectively improve the mass transfer efficiency, fully remove hydrogen sulfide and carbon dioxide, and effectively purify the syngas.

[0007] The technical solution of the present invention is as follows: A device for desulfurization and decarbonization of syngas is composed of a dust removal mechanism, an absorption mechanism, and a regeneration mechanism arranged in sequence. It is characterized in that: the dust removal mechanism includes a spin spray dust removal tower, the absorption mechanism includes a spin spray absorption tower, and the regeneration mechanism includes a spin spray regeneration tower; the spin spray dust removal tower, the spin spray absorption tower, and the spin spray regeneration tower are respectively composed of a tower body and a spin sprayer. At least one spin sprayer is arranged in the tower body, and multiple spin sprayers are connected in series or in parallel with each other.

[0008] A liquid inlet is arranged on the spin sprayer. A gas inlet is arranged tangentially along the spin sprayer above the liquid inlet, and a gas outlet is arranged at the center of the top of the spin sprayer; the spin sprayer below the liquid inlet is in a conical cylinder shape.

[0009] The dust removal mechanism further includes a filter. One end of the filter is communicated with the bottom of the tower body of the spin spray dust removal tower, and the other end of the filter is communicated with the liquid inlet of the spin sprayer of the spin spray dust removal tower through a delivery pump.

[0010] The absorption mechanism further includes a dehydration unit, a flash tank, an igniter, and a heat exchanger. The dehydration unit is communicated with the top of the tower body of the spin spray absorption tower; one end of the flash tank is communicated with the top of the tower body of the spin spray absorption tower; the top of the flash tank is connected to the igniter; the other end of the flash tank is communicated with the liquid inlet of the spin sprayer of the spin spray regeneration tower through a heat exchanger; the bottom of the tower body of the spin spray regeneration tower is sequentially communicated with the liquid inlet of the spin sprayer of the spin spray absorption tower through a heat exchanger, a water cooler, and a delivery pump.

[0011] The described dehydration unit includes one or a combination of more than one of at least one stage of centrifugal separator, gravity separator, wire mesh separator, and baffle separator.

[0012] The described regeneration mechanism further includes a reboiler, a reflux drum, and a sulfur Claus unit. One side of the reboiler is connected to the bottom of the body of the spin spray regeneration tower, and the other side of the reboiler is connected to the liquid inlet of the spin sprayer of the spin spray regeneration tower through a transfer pump; the side of the reflux drum is connected to the top of the body of the spin spray regeneration tower through a condenser, the bottom of the reflux drum is connected to the body of the spin spray regeneration tower above the spin sprayer through a transfer pump, and the top of the reflux drum is connected to the sulfur Claus unit.

[0013] A method for desulfurization and decarbonization of syngas, characterized in that it includes the following steps: Spin spray dust removal, spin spray absorption, and spin spray regeneration.

[0014] The described spin spray dust removal includes the following steps: The syngas is input from the gas inlet of the spin sprayer of the spin spray dust removal tower of the syngas desulfurization and decarbonization device, and industrial water is input from the liquid inlet of the spin sprayer of the spin spray dust removal tower: The industrial water washes the syngas in the swirling flow field inside the spin spray dust removal tower to promote the agglomeration and sedimentation of solid particles in the syngas to form a turbid liquid; the turbid liquid flows out from the bottom of the tower, and after passing through a filter, it is pumped into the spin spray dust removal tower again for recycling; the washed syngas is input into the spin spray absorption tower; The described spin spray absorption includes the following steps: The syngas is tangentially input from the gas inlet of the spin sprayer of the spin spray absorption tower; the lean amine solution is radially input from the liquid inlet of the spin sprayer of the spin spray absorption tower; the syngas forms a swirling flow field, shearing and atomizing the jet of the lean amine solution to form micron-sized droplets, and the swirling flow field evolves into a swirling turbulent flow field; in the intense turbulent flow field, the amine solution reacts with CO 2 、H 2 S to generate carbamate, removing CO 2 、H 2 S in the syngas; the purified syngas is transported from the top of the spin spray absorption tower to the dehydration unit, and is collected after dehydration; the rich amine solution after absorbing CO 2 、H 2 S flows from the bottom of the spin spray absorption tower to the flash tank, and after flashing, it is sent to the spin spray regeneration tower through heat exchange in a heat exchanger; the flash gas generated by the flash tank is sent to the igniter for combustion; The described spin spray regeneration includes the following steps: The flashed rich amine solution is sent to the spin spray regeneration tower to release CO 2 and H 2The acidic mixed gas of S, after being condensed at the top of the tower, is sent to the reflux drum. In the reflux drum, gas-liquid separation occurs. The gas enters the sulfur Claus unit, and the liquid refluxes to the top of the spin spray regeneration tower; the rich amine solution is desorbed to form a lean amine solution. The lean amine solution is split at the bottom of the spin spray regeneration tower. Part of the lean amine solution is cooled by a heat exchanger and a water cooler and pumped into the spin spray absorption tower; another part of the lean amine solution is heated by a reboiler and then returned to the spin spray regeneration tower.

[0015] The operating pressure drop of the spin sprayer of the single-stage spin spray absorption tower is 1 - 4 kPa, and the spray hole diameter is 0.8 - 2 mm.

[0016] The lean amine solution mentioned above includes a mixed solution of one or more of methyl diethanolamine (MDEA) with a mass concentration of 34%, ethanolamine (MEA), triethanolamine (TEA), diethylene glycol amine (DGA), diethanolamine (DEA), diisopropanolamine (DIPA), tert-butylaminoethoxyethanol (TBEE), piperazine (PZ), and water.

[0017] The rich amine solution is heated to 60 - 80 °C after heat exchange in the heat exchanger; the lean amine solution returned from the spin spray regeneration tower to the spin spray absorption tower is cooled to 40 - 50 °C by the water cooler; the regeneration temperature is 100 - 130 °C.

[0018] The intake gas flow rate of the syngas entering the spin spray absorption tower is 60 - 140 m³ / h, and the intake gas pressure is 6.4 - 6.7 Mpa; the gas-liquid ratio of the amine solution entering the spin spray absorption tower to the syngas is 2 - 10, and the inlet liquid temperature is less than or equal to 45 °C.

[0019] As a comparison, in the laboratory, the device for desulfurizing and decarbonizing syngas with a spin sprayer is respectively processed under the same throughput and the same raw material syngas as the traditional packed tower and plate tower. The experimental results are as follows: Comparative Experiment 1:

[0020] Table 1: Statistical Table of the Results of Comparative Experiment 1 Comparative Experiment 2

[0021] Table 2: Statistical Table of the Results of Comparative Experiment 2 As can be seen from Table 1 and Table 2 above, the contents of CO 2 and H 2 S in the syngas treated with the spin sprayer are significantly lower than those in the packed tower and the plate tower. More CO 2 and H 2 S in the syngas are absorbed in the spin sprayer, and the purification is better. Therefore, the mass transfer efficiency in the spin sprayer is higher.

[0022] The beneficial effects of the present invention are as follows: In the device and method for desulfurization and decarbonization of syngas, amine liquid is broken into micron-sized droplets in a spinning spray absorption tower. By using a swirling turbulent flow field that couples gas-phase swirling and liquid-phase jetting, a droplet dispersion system at the micron scale is constructed, greatly increasing the liquid-gas phase interface area and doubling the mass transfer area, which can effectively improve the absorption of CO 2 and H 2 S in the syngas and effectively improve the mass transfer efficiency. At the same time, a swirling turbulent flow field is generated in the syngas to increase the turbulence degree of the gas phase and the liquid phase. By combining the self-rotation and revolution of the droplets, the gas-liquid contact time is extended, further improving the mass transfer efficiency. The spinning sprayer can not only replace the conventional trays and packings, greatly reducing the volume of the tower equipment while doubling the mass transfer area, with the tower volume reduced by about 40%, and can be flexibly applied to the new construction of related enterprise devices and the renovation projects of old devices. Moreover, compared with a rotating packing tower, the process is simple and the energy consumption is reduced, which is suitable for the construction of new equipment. It solves the problem of low mass transfer efficiency existing in the existing desulfurization and decarbonization methods. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 is a schematic diagram of the process principle of the present invention; Figure 2 is a schematic diagram of the multi-stage series connection of the spinning sprayer of the present invention; Figure 3 is a schematic diagram of the principle of the spinning sprayer of the present invention.

[0024] In the figure: 1. Spinning spray dust removal tower, 2. Spinning spray absorption tower, 3. Spinning spray regeneration tower, 4. Filter, 5. Delivery pump, 6. Dewatering unit, 7. Flash tank, 8. Igniter, 9. Heat exchanger, 10. Water cooler, 11. Reboiler, 12. Reflux tank, 13. Sulfur Claus unit, 14. Condenser, 101. Tower body, 102. Spinning sprayer, 103. Liquid inlet, 104. Gas inlet, 105. Gas outlet. DETAILED DESCRIPTION OF THE INVENTION

[0025] The device for desulfurization and decarbonization of syngas is composed of a dust removal mechanism, an absorption mechanism, and a regeneration mechanism arranged in sequence. The dust removal mechanism removes particulate impurities in the syngas by dust removal; the absorption mechanism cooperates with amine liquid to desulfurize and decarbonize the syngas, absorbing and removing H 2 S and CO 2 in the syngas; the regeneration mechanism regenerates the amine liquid, converting the rich amine liquid into lean amine liquid, and the lean amine liquid absorbs H 2 S and CO 2 again, thereby recycling the amine liquid.

[0026] The dust removal mechanism includes a spin spray dust removal tower 1, the absorption mechanism includes a spin spray absorption tower 2, and the regeneration mechanism includes a spin spray regeneration tower 3; the spin spray dust removal tower 1, the spin spray absorption tower 2, and the spin spray regeneration tower 3 are respectively composed of a tower body 101 and a spin sprayer 102. At least one spin sprayer 102 is arranged in the tower body 101, and multiple spin sprayers 102 are connected in series or in parallel. The function of the spin sprayer is to generate a violent swirling turbulent flow field inside the spin sprayer 102, and generate a swirling flow field through the gas phase entering tangentially to cut and tear the liquid phase entering radially, so that the liquid phase is broken and atomized into droplets, thereby greatly increasing the gas-liquid mass transfer area when the liquid phase is broken and effectively improving the mass transfer efficiency; at the same time, under the push of the gas phase, the droplets are promoted to revolve while rotating, and the self-revolution coupling movement further strengthens the absorption reaction process, and further improves the mass transfer efficiency, removing particulate impurities, H 2 S and CO 2 concentration in the syngas is reduced to within the range permitted by the national standard through the absorption of amine solution, and at the same time, the regeneration efficiency of the amine solution is improved.

[0027] A liquid inlet 103 is arranged on the spin sprayer 102 to radially feed liquid into the spin sprayer 102 from the liquid inlet 103. A gas inlet 104 is arranged tangentially on the spin sprayer 102 above the liquid inlet 103 to tangentially introduce gas into the spin sprayer 102 from the gas inlet 104. A gas outlet 105 is arranged at the center of the top of the spin sprayer 102 to discharge the purified gas upward through the gas outlet 105. The spin sprayer 102 below the liquid inlet 103 is in a conical cylinder shape, and a liquid outlet is arranged at the bottom of the spin sprayer 102.

[0028] The dust removal mechanism further includes a filter 4. One end of the filter 4 is communicated with the bottom of the tower body 101 of the spin spray dust removal tower 1, and the other end of the filter 4 is communicated with the liquid inlet 103 of the spin sprayer 102 of the spin spray dust removal tower 1 through a delivery pump 5. The filter 4 is a combination of one or more of a centrifugal filter, a plate and frame filter press, a membrane filter, a bag filter, and a cartridge filter.

[0029] The absorption mechanism further includes a dehydration unit 6, a flash tank 7, an igniter 8, and a heat exchanger 9. The dehydration unit 6 is connected to the top of the tower body 101 of the spin spray absorption tower 2 to dehydrate through the dehydration unit 6 and remove the moisture in the syngas. One end of the flash tank 7 is connected to the top of the tower body 101 of the spin spray absorption tower 2; the top of the flash tank 7 is connected to the igniter 8; the other end of the flash tank 7 is connected to the liquid inlet 103 of the spin sprayer 102 of the spin spray regeneration tower 3 through the heat exchanger 9. The function of the flash tank 7 is to flash the rich amine liquid after absorbing the impurity gas in the syngas, thereby removing the insoluble gas and combustible gas entrained in the rich amine liquid, and burning it through the igniter 8, so as to avoid accidents during heating and regeneration in the regeneration mechanism and ensure the safety during regeneration. The bottom of the tower body 101 of the spin spray regeneration tower 3 is sequentially connected to the liquid inlet 103 of the spin sprayer 102 of the spin spray absorption tower 2 through the heat exchanger 9, a water cooler 10, and a transfer pump 5. The function of the heat exchanger 9 is to exchange heat between the rich amine liquid flowing from the flash tank 7 to the spin spray regeneration tower 3 and the lean amine liquid flowing from the spin spray regeneration tower 3 to the spin spray absorption tower 2 through the heat exchanger 9, heat the rich amine liquid, and cool the lean amine liquid.

[0030] The dehydration unit 6 includes one or a combination of at least one stage of centrifugal separator, gravity separator, wire mesh separator, and baffle separator. For example, the dehydration unit 6 is a single-stage wire mesh separator, or a combination of a single-stage gravity separator and a single-stage wire mesh separator in series, or a combination of multiple-stage centrifugal separators in parallel and a single-stage baffle separator in parallel. The dehydration rate is higher than 99.5%.

[0031] The regeneration mechanism further includes a reboiler 11, a reflux drum 12, and a sulfur Claus unit 13 (commercially available). One side of the reboiler 11 is connected to the bottom of the tower body 101 of the spin spray regeneration tower 3, and the other side of the reboiler 11 is connected to the liquid inlet 103 of the spin sprayer 102 of the spin spray regeneration tower 3 through a transfer pump 5; the side of the reflux drum 12 is connected to the top of the tower body 101 of the spin spray regeneration tower 3 through a condenser 14, the bottom of the reflux drum 12 is connected to the tower body 101 of the spin spray regeneration tower 3 above the spin sprayer 102 through a transfer pump 5, and the top of the reflux drum 12 is connected to the sulfur Claus unit 13. The function of the reboiler 11 is to heat the liquid through the reboiler 11, and through heating, the amine liquid undergoes a reverse reaction to decompose H 2 S and CO 2 , so that the rich amine liquid becomes lean amine liquid, and then the amine liquid is regenerated, so that the amine liquid can be reused. The function of the spin sprayer in the spin spray regeneration tower 3 is to form a swirling flow field through the spin sprayer, thereby crushing and atomizing the amine liquid, accelerating the decomposition and overflow of H 2 S and CO 2 , and improving the regeneration efficiency. The function of the condenser 14 is to condense the gas, and then the amine liquid formed by condensation in the gas is separated in the reflux drum 12, so as to recover the amine liquid and reduce the loss of amine liquid. The sulfur Claus unit 13 can treat H2 The S gas absorption reaction recovers sulfur elements and removes H in the gas. 2 For the S gas, the discharged gas is made harmless. Example 1

[0032] The syngas desulfurization and decarbonization method includes the following steps: The syngas desulfurization and decarbonization device adopts a single-stage swirl dust removal tower 1, a swirl absorption tower 2 and a swirl regeneration tower 3. The gas phase inlet is located at the top of the cylinder body. The aperture of the injection holes in the liquid inlet is 0.8 mm, and the number of injection holes is 80 (8 layers * 10 pieces / layer). The gas-liquid ratio of the syngas to the amine liquid is 2 - 6. The amine liquid is an aqueous solution of 34% methyl diethanolamine (MDEA) and 1% monoethanolamine (MEA) by mass concentration. The dehydration unit 6 adopts a wire mesh separator, and the filter 4 adopts a centrifugal filter.

[0033]

[0034] Table 3 shows the properties of the syngas before purification For the above syngas with a flow rate of 100 m 3 / h and a pressure of 6.4 MPa, it passes through the swirl dust removal tower 1 to remove solid particles in the gas, and enters the swirl absorption tower 2 together with the lean amine liquid (at 16 m 3 / h and a temperature of 45 °C) from the swirl regeneration tower 3. The syngas entering the swirl absorber 2 through the tangential inlet shears the lean amine liquid entering the swirl absorber 2 through the radial inlet. The gas phase and the liquid phase form a swirling turbulent field in the swirl absorber 2 of the swirl absorber 102. The droplet size distribution range of the liquid droplets after gas phase shearing is 400 - 800 μm (detected by a laser particle size analyzer). Gas-liquid mass transfer occurs in the swirling turbulent field, and the absorption liquid desulfurization and decarbonization reaction occurs. The CO 2 content of the purified syngas is 0.45%, and the H 2 S content is 4.2 mg / m 3 . The purified syngas enters the dehydration unit 6 with an in-built wire mesh separator from the top of the tower and is collected after dehydration. The rich amine liquid flows out from the bottom of the swirl absorption tower 2, enters the flash tank 7 for flashing, and the flash gas enters the igniter 8 for ignition and combustion. The rich amine liquid flowing out from the liquid phase outlet of the flash tank 7 passes through the heat exchanger 9, is heated after exchanging heat with the regenerated lean amine liquid, and enters the upper-middle inlet of the swirl regeneration tower 3.

[0035] The rich amine liquid is desorbed and regenerated in the swirl regeneration tower 3, and the CO 2 and H 2The acidic mixed gas is discharged from the top gas-phase outlet. The gas-phase outlet of the spin spray regeneration tower 3 is connected to the condenser 14. The reflux liquid is discharged from the bottom liquid-phase outlet of the reflux tank 12 and is conveyed back to the top of the spin spray regeneration tower 3 through the transfer pump 5. The bottom of the spin spray regeneration tower 3 is connected to the reboiler 11. Using saturated steam as the heat source, the rich amine liquid is heated in the reboiler 11 and discharged from the bottom outlet of the reboiler 11 and sent back to the spin spray regeneration tower 3. The lean amine liquid after being resolved in the spin spray regeneration tower 3 flows out from the middle and lower part, enters the heat exchanger 9 to cool down, realizing the recycling of the amine liquid. Example 2

[0036] The syngas desulfurization and decarbonization device uses the spin spray dust removal tower 1, the spin spray absorption tower 2 and the spin spray regeneration tower 3 with the spin sprayer 102 in a two-stage series connection. The spray hole diameter is 1.5 mm, and the number of spray holes is 80 (8 layers * 10 holes / layer). The gas-liquid ratio of the syngas to the amine liquid is 6 - 10. The amine liquid is an aqueous solution of 34% methyl diethanolamine (MDEA) and 1% monoethanolamine (MEA) by mass concentration. The dehydration unit 6 uses a wire mesh separator, and the filter 4 uses a centrifugal filter.

[0037]

[0038] Table 4 shows the properties of the syngas before purification For the above-mentioned syngas, with a flow rate of 100 m 3 / h and a pressure of 6.7 MPa, the solid particles in the gas are removed through the spin spray dust removal tower 1, and the lean amine liquid from the spin spray regeneration tower 3 (at 50 m 3 / h and a temperature of 45 °C) is input into the spin spray absorption tower 2. The syngas entering the spin sprayer 102 of the spin spray absorption tower 2 tangentially shears the lean amine liquid entering the spin sprayer 102 of the spin spray absorption tower 2 radially, and a swirling turbulent field is formed between the gas phase and the liquid phase in the spin sprayer 102 of the spin spray absorption tower 2. The droplet size distribution range of the liquid droplets after gas-phase shearing is 500 - 1000 μm, and gas-liquid mass transfer occurs in the swirling turbulent field, and the absorption liquid desulfurization and decarbonization reaction takes place. The CO 2 content of the purified syngas is 0.4%, and the H 2 S content is 4.8 mg / m 3 . The purified syngas enters the dehydration unit 6 with a built-in wire mesh separator from the top of the tower and is collected after dehydration. The rich amine liquid flows out from the bottom of the spin spray absorption tower 2, enters the flash tank 7 for flashing, and the flash gas enters the igniter 8 for ignition and combustion. The rich amine liquid flowing out from the liquid-phase outlet of the flash tank 7 passes through the heat exchanger 9, is heated after heat exchange with the regenerated lean amine liquid, and enters the upper-middle inlet of the spin spray regeneration tower 3.

[0039] The rich amine liquid is resolved and regenerated in the spin spray regeneration tower 3. The CO 2 and H 2The sour gas mixture is discharged from the top gas-phase outlet. The gas-phase outlet of the spin spray regeneration tower 3 is connected to the condenser 14. The reflux liquid is discharged from the bottom liquid-phase outlet of the reflux tank 12 and is transported back to the top of the spin spray regeneration tower 3 through the transfer pump 5. The bottom of the spin spray regeneration tower 3 is connected to the reboiler 11. Using saturated steam as the heat source, the rich amine liquid is heated in the reboiler 11 and discharged from the bottom outlet of the reboiler 11 and sent back to the spin spray regeneration tower 3. The lean amine liquid after being resolved in the spin spray regeneration tower 3 flows out from the middle and lower part and enters the heat exchanger 9 to be cooled, realizing the recycling of the amine liquid.

[0040] In the device and method for desulfurization and decarbonization of the synthesis gas, the amine liquid is broken into micron-sized droplets in the spin spray absorption tower 2. By adopting a swirl turbulent flow field coupling gas-phase swirl and liquid-phase jet, a micron-scale droplet dispersion system is constructed, greatly increasing the phase boundary area of the liquid, doubling the mass transfer area, and effectively improving the absorption of CO 2 and H 2 S in the synthesis gas, effectively improving the mass transfer efficiency. At the same time, a swirl turbulent flow field is generated in the synthesis gas, increasing the turbulence degree of the gas phase and the liquid phase. By combining the self-rotation and revolution movements of the droplets, the gas-liquid contact time is extended, further improving the mass transfer efficiency. The spin sprayer 102 can not only replace the conventional trays and packings, greatly reducing the volume of the tower equipment while doubling the mass transfer area. The tower volume is reduced by about 40%, and it can be flexibly applied to the new construction of relevant enterprise devices and the renovation projects of old devices. Moreover, compared with the rotating packing tower, the process is simple and the energy consumption is reduced, which is suitable for the construction of new equipment. It solves the problem of low mass transfer efficiency existing in the existing desulfurization and decarbonization methods.

Claims

1. A device for desulfurizing and removing carbon from synthesis gas, which is composed of a dust removal mechanism, an absorption mechanism and a regeneration mechanism arranged in sequence, and is characterized in that: The dust removal mechanism comprises a rotary spray dust removal tower (1), the absorption mechanism comprises a rotary spray absorption tower (2), and the regeneration mechanism comprises a rotary spray regeneration tower (3); the rotary spray dust removal tower (1), the rotary spray absorption tower (2), and the rotary spray regeneration tower (3) are respectively composed of a tower body (101) and a rotary sprayer (102); at least one rotary sprayer (102) is arranged in the tower body (101), and a plurality of rotary sprayers (102) are connected in series or in parallel.

2. The device for desulfurization and decarbonization of synthesis gas according to claim 1, characterized in that: The rotary sprayer (102) is provided with a liquid inlet (103), a gas inlet (104) is tangentially provided on the rotary sprayer (102) above the liquid inlet (103), and a gas outlet (105) is provided at the center of the top of the rotary sprayer (102); the rotary sprayer (102) below the liquid inlet (103) is in a conical cylindrical shape.

3. The device for desulfurization and decarbonization of synthesis gas according to claim 1, characterized in that: The dust removal mechanism further comprises a filter (4), one end of the filter (4) being in communication with the bottom of a tower body (101) of the rotary spray dust removal tower (1), and the other end of the filter (4) being in communication with a liquid inlet (103) of a rotary sprayer (102) of the rotary spray dust removal tower (1) via a delivery pump (5).

4. The device for desulfurization and decarbonization of synthesis gas according to claim 1, characterized in that: The absorption mechanism further comprises a dehydration unit (6), a flash tank (7), an igniter (8) and a heat exchanger (9); the dehydration unit (6) is connected to the top of the tower body (101) of the rotary spray absorption tower (2); one end of the flash tank (7) is connected to the top of the tower body (101) of the rotary spray absorption tower (2); the top of the flash tank (7) is connected to the igniter (8); the other end of the flash tank (7) is connected to the liquid inlet (103) of the rotary spray device (102) of the rotary spray regeneration tower (3) through the heat exchanger (9); the bottom of the tower body (101) of the rotary spray regeneration tower (3) is connected to the liquid inlet (103) of the rotary spray device (102) of the rotary spray absorption tower (2) through the heat exchanger (9), the water cooler (10) and the delivery pump (5) in sequence.

5. The device for desulfurization and decarbonization of synthesis gas according to claim 4, characterized in that: The dehydration unit (6) comprises at least one stage of a centrifugal separator, a gravity separator, a wire mesh separator and a baffle separator, or a combination of one or more of the above.

6. The device for desulfurization and decarbonization of synthesis gas according to claim 1, characterized in that: The regeneration mechanism further comprises a reboiler (11), a reflux tank (12) and a sulfur Claus unit (13); one side of the reboiler (11) is connected to the bottom of a tower body (101) of a rotary spray regeneration tower (3); the other side of the reboiler (11) is connected to a liquid inlet (103) of a rotary spray device (102) of the rotary spray regeneration tower (3) through a delivery pump (5); the side of the reflux tank (12) is connected to the top of the tower body (101) of the rotary spray regeneration tower (3) through a condenser (14); the bottom of the reflux tank (12) is connected to the tower body (101) of the rotary spray regeneration tower (3) above the rotary spray device (102) through a delivery pump (5); and the top of the reflux tank (12) is connected to the sulfur Claus unit (13).

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