CN219701552U - Energy-saving system for coupling methanol elution carbon flash steam and dense gas combined alkali preparation - Google Patents
Energy-saving system for coupling methanol elution carbon flash steam and dense gas combined alkali preparation Download PDFInfo
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- CN219701552U CN219701552U CN202321013986.7U CN202321013986U CN219701552U CN 219701552 U CN219701552 U CN 219701552U CN 202321013986 U CN202321013986 U CN 202321013986U CN 219701552 U CN219701552 U CN 219701552U
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- 239000003513 alkali Substances 0.000 title claims abstract description 36
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 14
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 14
- 230000008878 coupling Effects 0.000 title claims abstract description 14
- 238000010168 coupling process Methods 0.000 title claims abstract description 14
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 14
- 238000002360 preparation method Methods 0.000 title claims abstract description 14
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims description 81
- 238000010828 elution Methods 0.000 title description 5
- 239000007791 liquid phase Substances 0.000 claims abstract description 41
- 239000012071 phase Substances 0.000 claims abstract description 39
- 238000005406 washing Methods 0.000 claims abstract description 38
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 37
- 230000023556 desulfurization Effects 0.000 claims abstract description 37
- 238000003763 carbonization Methods 0.000 claims abstract description 29
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 24
- 230000008929 regeneration Effects 0.000 claims abstract description 24
- 238000011069 regeneration method Methods 0.000 claims abstract description 24
- 238000005261 decarburization Methods 0.000 claims abstract description 23
- 238000000746 purification Methods 0.000 claims abstract description 15
- 239000007788 liquid Substances 0.000 claims description 27
- 239000000463 material Substances 0.000 claims description 15
- 229910052717 sulfur Inorganic materials 0.000 claims description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 239000011593 sulfur Substances 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 37
- 229910021529 ammonia Inorganic materials 0.000 abstract description 18
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 239000007789 gas Substances 0.000 description 87
- 238000000034 method Methods 0.000 description 13
- 239000000243 solution Substances 0.000 description 13
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 8
- 238000004064 recycling Methods 0.000 description 7
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 238000005262 decarbonization Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 235000019270 ammonium chloride Nutrition 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000012267 brine Substances 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000001354 calcination Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 3
- 235000017557 sodium bicarbonate Nutrition 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000012265 solid product Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 238000011278 co-treatment Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 230000037390 scarring Effects 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
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Abstract
The utility model discloses an energy-saving system for coupling methanol-eluted carbon flash steam and concentrated gas combined alkali preparation, belonging to synthesisThe ammonia combined alkali field comprises a washing tower provided with a lower desulfurization section and an upper decarburization section, a first flash tank with a liquid phase inlet connected with a liquid phase outlet of the upper decarburization section, a second flash tank with a liquid phase inlet connected with a liquid phase outlet of the lower desulfurization section, a desulfurization tower, a carbonization tower with a gas phase inlet connected with a gas phase outlet of the first flash tank and a gas phase outlet of the desulfurization tower, a purification tower with a gas phase outlet connected with a gas phase inlet of the lower desulfurization section through a supercharger, a low-pressure regeneration system with an inlet connected with the second flash tank and the liquid phase outlet of the desulfurization tower, auxiliary equipment and the like; the liquid phase inlet of the desulfurizing tower is connected with the liquid phase outlet of the first flash tank, and the gas phase inlet is connected with the gas phase outlet of the second flash tank. The utility model omits the CO of the traditional combined concentrated gas alkali production system 2 The compressor also reduces the power consumption of the flash gas booster by 70-90%, and reduces the power consumption of the system operation.
Description
Technical Field
The utility model relates to the technical field of synthesis of ammonia combined alkali, in particular to an energy-saving system for coupling methanol eluting carbon flash steam and concentrated gas combined alkali preparation.
Background
By using CO as a dense gas 2 The synthesis ammonia combined alkali process for preparing alkali generally adopts low-pressure pure CO produced by regeneration of decarbonization section of synthesis ammonia system 2 ，CO 2 Pressurizing to 0.3-0.6MPa for alkali production by a compressor, and reacting with ammonia brine in a carbonization tower to prepare NaHCO 3 ，NaHCO 3 Calcining to obtain product Na 2 CO 3 . In the production process of synthetic ammonia, in order to avoid H in raw material gas in decarburization process of synthetic ammonia system 2 Loss of CO and CO removal 2 The rich liquid is generally subjected to flash evaporation under pressure to ensure that H with low solubility in the decarbonizing liquid 2 The CO is flash separated in advance and recycled. But the flash process is accompanied by a large amount of CO 2 Flash of CO in flash gas 2 The content is up to 70-90%, resulting in a significant increase in flash gas recycle compressor power consumption and due to CO 2 Is circulated through (a)The operating load of the decarburization tower is also increased.
The specific flow of the conventional dense gas combined alkali production system is shown in fig. 2:
the shift gas enters the desulfurization section at the lower part of the washing tower 1, and the CO-rich gas from the upper decarburization section 2 Methanol is used for washing, H in gas is removed 2 S is removed cleanly, then the gas enters an upper decarburization section, and CO is removed after washing by decarbonized methanol lean solution 2 Until the purifying requirement is met, the purified gas from the top of the washing tower 1 goes to a rear working section;
h-free upper decarbonization section and lower desulfurization section of the scrubber 1 2 S methanol rich liquid and H-containing 2 The S methanol rich solution respectively enters a first flash tank 2 and a second flash tank 3, and the flash liquid contains H 2 The flash gas of CO and the flash gas of the pressure reducing agent are combined, the pressure reducing agent is removed by a supercharger 11, pressurized and returned to the washing tower 1 for recycling, the methanol rich liquid after flash evaporation is respectively sent to the low-pressure regeneration system 8, and H-containing liquid is discharged from the low-pressure regeneration system 8 2 S and CO 2 The methanol lean solution regenerated from the low-pressure regeneration system 8 is sent to the decarbonization section at the upper part of the washing tower 1 after passing through the circulating pump 9, and the low-pressure CO is produced in the acid gas sulfur removal recovery section 2 Part of the waste water is pressurized by a compressor 10 and then is decarbonized by a tower 5, and the rest of the waste water is sent to users or empties such as urea, coal conveying working sections and the like. Low pressure CO 2 And reacting with ammonia brine in a carbonization tower 5 to generate sodium bicarbonate and ammonium chloride, processing materials at the lower part of the carbonization tower in a centrifugal machine 7, removing the solid product sodium bicarbonate from a calcination working section, and recycling mother liquor after separating ammonium chloride through ammonia absorption and salt dissolution. The tail gas at the top of the carbonization tower 5 is purified by a purification tower 6, the tail gas is directly discharged after being washed by washing water in the purification tower 6, and the washing liquid at the bottom is used for removing salt or absorbing ammonia.
Disclosure of Invention
The utility model aims to solve the technical problem of providing an energy-saving system for coupling methanol elution carbon flash steam and concentrated gas combined alkali preparation, which fully utilizes the pressure of the flash steam and combines the combined alkali preparation system to perform CO 2 The requirement of the gas quantity is properly controlled to ensure that CO in the flash steam 2 The gas quantity meets the alkali making requirement.
In order to solve the technical problems, the utility model adopts the following technical scheme:
an energy-saving system for coupling methanol eluting carbon flash steam and concentrated gas combined alkali preparation comprises a washing tower, a first flash tank, a second flash tank, a carbonization tower, a purification tower, a low-pressure regeneration system, a centrifugal machine, a circulating pump and connecting pipelines; the washing tower comprises a lower desulfurization section and an upper decarburization section; the liquid phase inlet of the first flash tank is connected with the liquid phase outlet of the upper decarburization section; the liquid phase inlet of the second flash tank is connected with the liquid phase outlet of the lower desulfurization section, and the system further comprises a desulfurization tower; the liquid phase inlet of the desulfurizing tower is connected with the bottom liquid phase outlet of the first flash tank, and the gas phase inlet of the desulfurizing tower is connected with the upper gas phase outlet of the second flash tank; the upper gas phase outlet of the first flash tank and the upper gas phase outlet of the desulfurizing tower are connected with the gas phase inlet of the carbonization tower; the bottom liquid phase outlet of the second flash tank and the bottom liquid phase outlet of the desulfurizing tower are connected with the inlet of the low-pressure regeneration system; the low-pressure regeneration system regenerates lean methanol liquid and is connected with a liquid phase inlet of the upper decarburization section of the washing tower through a circulating pump, and regenerates generated CO 2 The gas is connected with the user or is exhausted; h-containing of the low pressure regeneration system 2 S and CO 2 Is connected with a sulfur recovery working section; the top gas phase outlet of the purifying tower is connected with the gas phase inlet of the lower desulfurization section of the washing tower; and a supercharger is arranged on a pipeline of the gas phase outlet at the top of the purifying tower connected with the gas phase inlet of the lower desulfurization section of the washing tower.
The technical scheme of the utility model is further improved as follows: the liquid phase outlet ends at the bottoms of the lower desulfurization section, the upper decarburization section, the first flash tank, the second flash tank, the desulfurization tower and the purification tower are respectively provided with a valve for adjusting the flow of materials in the pipeline according to the liquid level of the equipment.
The technical scheme of the utility model is further improved as follows: the bottom material outlet end of the carbonization tower is provided with a centrifugal machine capable of carrying out solid-liquid separation, and the bottom material outlet end of the carbonization tower is also provided with a valve for adjusting the material flow in the pipeline according to the liquid level of the equipment.
The technical scheme of the utility model is further improved as follows: the first flash tank, theThe pressure of the second flash tank and the desulfurizing tower are used for carrying out CO treatment according to the combined alkali working section 2 The amount is set to 0.5-2.0Mpa.
By adopting the technical scheme, the utility model has the following technical progress:
1. according to the utility model, the pressure of the first flash tank and the pressure of the second flash tank are regulated, the desulfurizing tower is arranged behind the second flash tank, and the H-free flash tank is utilized 2 The methanol rich liquid of S carries out desulfurization on flash gas from the second flash tank, the first flash gas and the desulfurized second flash gas are converged and then enter a carbonization tower to react with ammonia brine, and the H-containing gas is discharged from a purification tower 2 The tail gas of CO is returned to the washing tower for recycling through the supercharger, so that the whole system does not need to be provided with the CO of the traditional combined concentrated gas alkali making system 2 The compressor saves one-time investment and reduces the power consumption of the system.
2. The utility model uses CO in the first flash steam and the second flash steam 2 Unreacted H as raw material of alkali producing system 2 The CO is returned to the washing tower through the supercharger for recycling, so that the power consumption of the methanol-eluted sulfur decarbonization flash gas circulation supercharger in the synthetic ammonia system is reduced by 70-90%, and the investment and the running power consumption of the flash gas circulation supercharger are greatly saved.
3. The flash evaporation gas used as carbonized raw material gas has a small amount of H 2 Non-reactive gases such as CO and the like can increase the stirring effect of the gases in the carbonization tower of the combined alkali system on the liquid, increase the contact opportunity of the gases and the liquid, improve the mass transfer efficiency and reduce the scarring probability of the carbonization tower.
Drawings
For a clearer description of embodiments of the utility model or of the solutions of the prior art, the drawings that are used in the description of the embodiments or of the prior art will be briefly described, it being obvious that the drawings in the description below are some embodiments of the utility model, and that other drawings can be obtained according to these drawings without inventive faculty for a person skilled in the art;
FIG. 1 is a schematic diagram of an energy-saving system and process for coupling methanol-eluting carbon flash steam with a dense gas for combined alkali production according to an embodiment of the present utility model;
FIG. 2 is a schematic diagram of a conventional combined dense gas alkali making system and process in the background of the utility model;
wherein, 1, a washing tower; 2. a first flash tank; 3. a second flash drum; 4. a desulfurizing tower; 5. a carbonization tower; 6. a purifying tower; 7. a centrifuge; 8. a low pressure regeneration system; 9. a circulation pump; 10. a compressor; 11. a supercharger.
Detailed Description
It is noted that the terms "comprises" and "comprising," and any variations thereof, in the description and claims of the present utility model and in the foregoing figures, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed or inherent to such process, method, article, or apparatus.
The embodiment of the utility model solves the problem that the flash evaporation process is accompanied with a large amount of CO in the prior art by providing the energy-saving system for the coupling of the methanol elution carbon flash vapor and the concentrated gas combined alkali preparation 2 Flash of CO in flash gas 2 The content is up to 70-90%, resulting in a significant increase in flash gas recycle compressor power consumption and due to CO 2 And the operation load of the decarburization tower is increased. "problems, the general idea is: and a desulfurization tower is arranged between the low-pressure regeneration system and the back of the first flash tank and the second flash tank, the pressure of the first flash tank, the second flash tank and the desulfurization tower is regulated, the flash gas quantity meets the alkali making requirement, the flash gas is directly sent into the carbonization tower for reaction, a compressor behind the low-pressure regeneration system is eliminated, and the tail gas from the purification tower is returned to the washing tower for recycling through a booster.
The utility model is described in further detail below with reference to the attached drawings and examples:
as shown in FIG. 1, the embodiment provides a methanol-eluted carbon flash gas and dense gas combinationThe energy-saving system for coupling the combined alkali comprises a washing tower 1, a first flash tank 2, a second flash tank 3, a carbonization tower 5, a purification tower 6, a low-pressure regeneration system 8, a centrifugal machine 7, a circulating pump 9 and connecting pipelines; the washing tower 1 comprises a lower desulfurization section and an upper decarburization section; the liquid phase inlet of the first flash tank 2 is connected with the liquid phase outlet of the upper decarburization section; the liquid phase inlet of the second flash tank 3 is connected with the liquid phase outlet of the lower desulfurization section, and the system further comprises a desulfurization tower 4; the liquid phase inlet of the desulfurizing tower 4 is connected with the bottom liquid phase outlet of the first flash tank 2, and the gas phase inlet of the desulfurizing tower 4 is connected with the upper gas phase outlet of the second flash tank 3; the upper gas phase outlet of the first flash tank 2 and the upper gas phase outlet of the desulfurizing tower 4 are connected with the gas phase inlet of the carbonization tower 5; the bottom liquid phase outlet of the second flash tank 3 and the bottom liquid phase outlet of the desulfurizing tower 4 are connected with the inlet of the low-pressure regeneration system 8; the lean liquid outlet of the low-pressure regeneration system 8 is connected with the liquid phase inlet of the upper decarburization section of the washing tower 1 through a circulating pump 9, and low-pressure CO 2 The outlet is connected with a user or is empty; h-containing of the low pressure regeneration system 8 2 S and CO 2 Is connected with a sulfur recovery working section; the top gas phase outlet of the purifying tower 6 is connected with the gas phase inlet of the lower desulfurization section of the washing tower 1; a supercharger 11 is arranged on a pipeline of the top gas phase outlet of the purifying tower 6 connected with the gas phase inlet of the lower desulfurization section of the washing tower 1.
Further, valves for adjusting the material flow in the pipeline according to the liquid level of the equipment are arranged at the liquid phase outlet ends at the bottoms of the lower desulfurization section, the upper decarburization section, the first flash tank 2, the second flash tank 3, the desulfurization tower 4 and the purification tower 6. The safety and stability of the system are further ensured by the arrangement of the valves.
Further, a centrifugal machine 7 capable of carrying out solid-liquid separation is arranged at the bottom material outlet end of the carbonization tower 5, and a valve for adjusting the material flow in the pipeline according to the liquid level of the equipment is also arranged at the bottom material outlet end of the carbonization tower 5.
The technological process of the energy-saving system for combining methanol elution carbon flash steam and dense gas alkali preparation coupling is as follows:
transformationThe gas enters the lower desulfurization section of the washing tower 1 and is rich in CO from the upper decarburization section 2 Methanol is washed, H in the converted gas is changed 2 S is removed cleanly, then the gas enters an upper decarburization section, and CO is removed after washing by decarbonized methanol lean solution 2 The purified gas from the top of the washing tower 1 goes to the subsequent working section until the requirement of the conversion gas purification is met;
h-free removal from the upper decarbonization section of the scrubber 1 2 S, the methanol rich solution enters a first flash tank 2; h-containing gas coming out of the desulfurization section at the lower part of the washing tower 1 2 The S methanol rich solution enters a second flash tank 3, and H is contained from a gas phase outlet at the upper part of the first flash tank 2 2 A first flash decarbonizing column 5 for CO; h-containing gas exiting from the upper gas phase outlet of the second flash tank 3 2 、CO、H 2 S second flash steam is sent to the desulfurizing tower 4, and H-free liquid phase is discharged from the liquid phase outlet at the bottom of the first flash tank 2 2 S, washing and desulfurizing the methanol rich solution in the desulfurizing tower 4, and then removing the gas from the carbonizing tower 5; in the carbonization tower 5, the first flash vapor from the gas phase outlet at the upper part of the first flash tank 2 and the gas after desulfurization from the gas phase outlet at the upper part of the desulfurization tower 4 react with ammonia brine to generate ammonium chloride and sodium bicarbonate, the lower material from the material outlet at the bottom of the carbonization tower 5 is treated by a centrifugal machine 7, the solid product sodium bicarbonate is removed to a calcination working section, and the mother solution is recycled after ammonia absorption, salt dissolution and ammonium chloride separation; the tail gas from the gas phase outlet at the top of the carbonization tower 5 is purified by the purification tower 6, the tail gas is washed by washing water in the purification tower 6, pressurized by the booster 11 and recycled by the washing tower 1, and the washing liquid from the liquid phase outlet at the bottom of the purification tower 6 is used for removing salt or absorbing ammonia;
h-containing liquid exiting from bottom liquid outlet of second flash tank 3 2 The S methanol rich liquid and the washing liquid from the liquid phase outlet at the bottom of the desulfurizing tower 4 are returned to the low-pressure regeneration system 8, and H is contained after being treated by the low-pressure regeneration system 8 2 S and CO 2 The lean solution treated by the low-pressure regeneration system 8 is sent to the upper decarburization section of the washing tower 1 after passing through the circulating pump 9, and low-pressure CO 2 To the user or to the air.
Further, the pressures of the first flash tank 2, the second flash tank 3 and the desulfurizing tower 4According to CO of CO 2 The amount is set to 0.5-2.0Mpa.
Working principle:
as shown in FIG. 2, the upper decarburization section and the lower desulfurization section (methanol wash section) of the scrubber 1 are operated to remove CO from the shift gas 2 (used for urea production or alkali production, etc.) and H 2 S and other impurities. The content (volume fraction) of the converted gas (pressure 3.2-5.8 MPa) components is as follows: CO 2 45% of H 2 S0.22%, CO 0.4%, H 2 54% of H in the physical absorption process of the methanol barren solution 2 Dissolving the ammonia and CO in methanol solution, and flash evaporating H under pressure to recover the effective ammonia gas 2 And desorption and separation of CO from the methanol solution (the functions of the first flash tank 2 and the second flash tank 3), but a large amount of CO is accompanied in the flash evaporation process 2 The desorption accounts for 70-90% of the flash vapor volume fraction, and the flash gas pressure is generally 0.9-1.6MPa, so that the supercharger 11 is required to boost to about 3.2-5.8MPa for recycling in the system. CO from the low pressure regeneration system 8 2 The pressure of (2) is 0.12 MPa, and the pressure is adjusted to be 0.3-0.6MPa in the carbonization tower 5 by the compressor 10.
As shown in FIG. 1, the utility model is based on the CO required by the combined alkali working section 2 The pressure of the first flash tank 2 and the second flash tank 3 is regulated to be 0.6-1.6 Mpa (originally 0.9-1.6 Mpa), so that the discharged flash gas not only meets the requirement of combined alkali on CO 2 The pressure can be adjusted to 0.3-0.6MPa to match the pressure of 0.3-0.6MPa required by alkali preparation, and CO is contained 2 、H 2 Directly sending the flash gas of CO to carbonization to prepare alkali, and CO 2 All are reacted in a carbonization tower 5 to finally prepare the product sodium carbonate, and the ammonia synthesis effective gas H in the tail gas of the carbonization tower 5 2 After being washed and purified by water, CO is pressurized to about 3.2-5.8MPa by the supercharger 11 and then returned to the system for recycling, so that the load of the supercharger 11 is reduced by 70-90% compared with the traditional process shown in figure 2. Because of the second flash drum 3 there will be H 2 S is released, so a desulfurizing tower 4 is added for further desulfurization.
Through accounting: the system shown in FIG. 2 is calculated by a device for synthesizing ammonia with annual output of 60 ten thousand tons for enterprises and circulatedThe power of the ring booster 11 is 630kw, the ring booster is produced according to 330 days in one year, and 630 multiplied by 24 multiplied by 330= 4989600 DEG, so that the technical scheme provided by the utility model can save 3492720-4490640 DEG electricity each year by saving 70-90% of power consumption of the booster, save one investment of the compressor 10, and effectively reduce the production cost for enterprises. Meanwhile, the CO is not required to be arranged in the combined alkali working section 2 The compressor saves investment and has huge running cost.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (4)
1. An energy-saving system for combined alkali preparation coupling of methanol eluting carbon flash steam and dense gas comprises a washing tower (1), a first flash tank (2), a second flash tank (3), a carbonization tower (5), a purification tower (6), a low-pressure regeneration system (8), a centrifuge (7), a circulating pump (9) and connecting pipelines; the washing tower (1) comprises a lower desulfurization section and an upper decarburization section; the liquid phase inlet of the first flash tank (2) is connected with the liquid phase outlet of the upper decarburization section; the liquid phase inlet of the second flash tank (3) is connected with the liquid phase outlet of the lower desulfurization section, and is characterized in that: the system further comprises a desulfurizing tower (4); the liquid phase inlet of the desulfurizing tower (4) is connected with the bottom liquid phase outlet of the first flash tank (2), and the gas phase inlet of the desulfurizing tower (4) is connected with the upper gas phase outlet of the second flash tank (3); the upper gas phase outlet of the first flash tank (2) and the upper gas phase outlet of the desulfurizing tower (4) are connected with the gas phase inlet of the carbonization tower (5); the bottom liquid phase outlet of the second flash tank (3) and the bottom liquid phase outlet of the desulfurizing tower (4) are connected with the inlet of the low-pressure regeneration system (8); the low pressure is used againThe regenerated lean methanol liquid of the regeneration system (8) is connected with the liquid phase inlet of the upper decarburization section of the washing tower (1) through a circulating pump (9), and the regenerated CO is produced 2 The gas is connected with the user or is exhausted; h-containing of the low pressure regeneration system (8) 2 S and CO 2 Is connected with a sulfur recovery working section; the top gas phase outlet of the purifying tower (6) is connected with the gas phase inlet of the lower desulfurization section of the washing tower (1); a supercharger (11) is arranged on a pipeline of the top gas phase outlet of the purifying tower (6) connected with the gas phase inlet of the lower desulfurization section of the washing tower (1).
2. The energy-saving system for combined alkali preparation and coupling of methanol-eluting carbon flash steam and dense gas according to claim 1, wherein the energy-saving system is characterized in that: the bottom liquid phase outlet ends of the lower desulfurization section, the upper decarburization section, the first flash tank (2), the second flash tank (3), the desulfurization tower (4) and the purification tower (6) are respectively provided with a valve for adjusting the material flow in the pipeline according to the liquid level of the equipment.
3. The energy-saving system for combined alkali preparation and coupling of methanol-eluting carbon flash steam and dense gas according to claim 1, wherein the energy-saving system is characterized in that: the bottom material outlet end of the carbonization tower (5) is provided with a centrifugal machine (7) capable of carrying out solid-liquid separation, and the bottom material outlet end of the carbonization tower (5) is also provided with a valve for adjusting the material flow in the pipeline according to the liquid level of the equipment.
4. The energy-saving system for combined alkali preparation and coupling of methanol-eluting carbon flash steam and dense gas according to claim 1, wherein the energy-saving system is characterized in that: the pressures of the first flash tank (2), the second flash tank (3) and the desulfurizing tower (4) are all used for carrying out CO according to a combined alkali working section 2 The amount is set to 0.5-2.0Mpa.
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| CN202321013986.7U CN219701552U (en) | 2023-04-28 | 2023-04-28 | Energy-saving system for coupling methanol elution carbon flash steam and dense gas combined alkali preparation |
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| CN202321013986.7U CN219701552U (en) | 2023-04-28 | 2023-04-28 | Energy-saving system for coupling methanol elution carbon flash steam and dense gas combined alkali preparation |
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