CN113599978A - Anhydrous low-temperature methanol washing device and production method - Google Patents
Anhydrous low-temperature methanol washing device and production method Download PDFInfo
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- CN113599978A CN113599978A CN202111027365.XA CN202111027365A CN113599978A CN 113599978 A CN113599978 A CN 113599978A CN 202111027365 A CN202111027365 A CN 202111027365A CN 113599978 A CN113599978 A CN 113599978A
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Abstract
本发明属于一种无水型低温甲醇洗装置以及生产方法，包括原料气管道以及甲醇洗涤塔，所述原料气管道通过原料气脱水单元与甲醇洗涤塔的原料气进口相连，甲醇洗涤塔的顶部与净化气管网相连；甲醇洗涤塔底部的液相出口通过富甲醇处理单元与甲醇洗涤塔中上部的贫甲醇喷淋管道进口相连；具有结构简单、设计合理、通过原料气脱水单元将原料气中的水分完全脱除，并在甲醇洗涤塔中通过贫甲醇液进行喷淋，实现了贫甲醇/富甲醇/循环甲醇中的水含量小于0.01％的特点，从而实现了避免相关设备都到腐蚀，节省原料气甲醇喷淋装置和甲醇水分离塔的购置成本，以及省去了后续工艺中甲醇和水的分离的优点。
The invention belongs to an anhydrous low-temperature methanol washing device and a production method, comprising a raw material gas pipeline and a methanol washing tower. It is connected with the purification gas pipe network; the liquid phase outlet at the bottom of the methanol washing tower is connected with the inlet of the lean methanol spraying pipe in the upper part of the methanol washing tower through the rich methanol processing unit; The water in the methanol washing tower is completely removed, and it is sprayed through the lean methanol liquid in the methanol washing tower, so that the water content in the lean methanol/rich methanol/circulating methanol is less than 0.01%, so as to avoid the corrosion of the related equipment. It saves the purchase cost of the raw gas methanol spray device and the methanol water separation tower, and saves the advantages of separating methanol and water in the subsequent process.
Description
Technical Field
The invention belongs to the technical field of gas purification, and particularly relates to an anhydrous low-temperature methanol washing device and a production method for removing carbon dioxide, hydrogen sulfide and other impurity gases in process gas by low-temperature methanol washing.
Background
The low-temperature methanol washing technology is widely applied to removal of acid gases such as carbon dioxide, hydrogen sulfide and the like in gas industry due to the technical advantages of the low-temperature methanol washing technology. In the low-temperature methanol washing process, low-temperature methanol absorbs acid gases such as carbon dioxide, hydrogen sulfide and the like to become methanol-rich liquid, and the methanol-rich liquid has strong acidity; particularly, when the methanol-rich liquid contains water, the acidity and the corrosivity of the methanol-rich liquid are increased, so that the corrosion of internal parts and inner walls of equipment is caused, and the defects of falling of a tower tray, blockage of a methanol-rich filter and the like can be caused in serious conditions, so that the production safety and the stable operation are not facilitated. The conventional low-temperature methanol washing process absorbs moisture in feed gas in a methanol spraying mode to obtain hydrous methanol, the hydrous methanol is rectified in a methanol-water separation tower, methanol steam is obtained at the tower top, methanol-containing wastewater is obtained at the tower bottom, the methanol and water are extremely difficult to be completely separated, the methanol steam brings water into circulating methanol, so that poor methanol at the tower top of the methanol washing tower contains 0.1-0.5% of moisture, and finally the acidity and the corrosivity of the rich methanol water are enhanced.
Disclosure of Invention
The invention aims to overcome the defects in the prior art, and provides the anhydrous low-temperature methanol washing device which is simple in structure and reasonable in design, completely removes the moisture in the raw material gas through the raw material gas dehydration unit, sprays the raw material gas in the methanol washing tower through the poor methanol solution, and realizes that the water content in the poor methanol/rich methanol/circulating methanol is less than 0.01 percent, and the production method.
The purpose of the invention is realized as follows:
a non-water type low-temperature methanol washing device comprises a raw material gas pipeline and a methanol washing tower, wherein the raw material gas pipeline is connected with a raw material gas inlet of the methanol washing tower through a raw material gas dehydration unit, and the top of the methanol washing tower is connected with a purified gas pipe network; and a liquid phase outlet at the bottom of the methanol washing tower is connected with a poor methanol spray pipeline inlet at the middle upper part of the methanol washing tower through a rich methanol treatment unit.
Preferably, the feed gas dehydration unit comprises at least one dehydration section; in the case of a plurality of dewatering units, the plurality of dewatering units are connected in series.
Preferably, the dehydration part comprises a precooler and a water separation tank connected with the precooler, and the bottom of the water separation tank is provided with a condensate recovery tank.
Preferably, the dewatering section comprises at least one regenerated molecular sieve assembly, and when there are a plurality of regenerated molecular sieve assemblies, the plurality of regenerated molecular sieve assemblies are connected in parallel.
Preferably, the regenerated molecular sieve component comprises a regenerated molecular sieve, the bottom of the regenerated molecular sieve is connected with a feed gas pipeline through a first tee joint and a first valve, the top of the regenerated molecular sieve is connected with an air outlet pipeline through a second tee joint and a second valve, the first tee joint is connected with a molecular sieve regenerated air outlet system through a third valve, and the second tee joint is connected with a molecular sieve regenerated air storage tank through a fourth valve.
Preferably, the raw material gas dehydration unit comprises a precooler connected with a raw material gas pipeline, an outlet of the precooler is connected with the regenerated molecular sieve through a water separation tank, a first valve and a first tee joint, and an outlet of the regenerated molecular sieve is connected with a raw material gas inlet of the methanol washing tower through a second tee joint, a second valve and a shell pass of the raw material gas cooler; the number of the regenerated molecular sieve components is two.
Preferably, the rich methyl alcohol processing unit includes the middling pressure flash column that links to each other with methyl alcohol washing tower bottom liquid phase export, and the liquid phase export of middling pressure flash column bottom links to each other with methyl alcohol analytic tower, and the liquid phase export of methyl alcohol analytic tower bottom passes through methyl alcohol cooler tube side and methyl alcohol pump and links to each other with methyl alcohol regeneration tower, and the liquid phase export of methyl alcohol regeneration tower bottom passes through poor methyl alcohol cooler, poor methyl alcohol jar, poor methyl alcohol pump and methyl alcohol cooler shell side and links to each other with poor methyl alcohol spray piping import.
Preferably, a gas phase outlet at the top of the medium-pressure flash tower is connected with a shell pass inlet of a raw material gas cooler through a circulating gas compressor; a gas phase outlet at the top of the methanol desorption tower is connected with a desorption gas pipe network through a feed gas cooler tube side; and a gas phase outlet at the top of the methanol regeneration tower is connected with an acid gas treatment device.
A production method of an anhydrous low-temperature methanol washing device comprises the following steps:
step 1: the raw material gas in the raw material gas pipeline is cooled by a precooler and then enters a water separation tank for gas-liquid separation, and the liquid phase after the gas-liquid separation enters a condensate recovery device; the temperature of the feed gas is as follows: 30-40 ℃, pressure: 4.0-6.5MPa, and the mole fraction of water is 0.1% -0.2%; the temperature of the feed gas at the outlet of the precooler 2 is as follows: the cold source of the precooler is lithium bromide or ammonia cold at 5-10 ℃;
step 2: the raw material gas after gas-liquid separation enters a regenerated molecular sieve through a first valve for re-dehydration, and the raw material gas after re-dehydration enters the shell pass of a raw material gas cooler through a second tee joint and a second valve; the water content in the feed gas passing through the outlet of the regenerated molecular sieve is less than 1 ppm;
and step 3: the raw material gas passing through the shell pass of the raw material gas cooler is cooled and then enters a methanol washing tower, the poor methanol entering from an inlet of a poor methanol spraying pipeline is sprayed, the sprayed gas phase enters a purified gas pipe network, and the methanol-rich liquid at the bottom of the methanol washing tower enters a medium-pressure flash tower through a liquid phase outlet at the bottom of the methanol washing tower; the temperature of the raw material gas at the shell pass outlet of the raw material gas cooler is as follows: -10 to-20 ℃;
and 4, step 4: the methanol-rich liquid solution enters a medium-pressure flash tower to be subjected to medium-pressure flash evaporation, steam subjected to medium-pressure flash evaporation is pressurized by a circulating gas compressor and then returns to the shell pass of the raw material gas cooler, and the step 3 is repeated; the liquid phase after medium-pressure flash evaporation enters a methanol desorption tower; the flash pressure of the medium-pressure flash tower is as follows: 1.2-1.7 MPa; the circulating gas compressor is a multi-stage centrifugal compressor with an interstage circulating water cooler, and the temperature of flash steam at the outlet of the circulating gas compressor is 20-40 ℃;
and 5: the liquid phase after medium-pressure flash evaporation enters a methanol analysis tower for analysis, and the gas phase enters a raw material gas cooler tube pass through a gas phase outlet at the top of the methanol analysis tower to exchange heat with raw material gas of a shell pass of the raw material gas cooler tube pass and then enters an analysis gas pipe network; the bottom pressure of the methanol desorption tower is 0.05-0.3 MPa; the temperature of the gas to be analyzed passing through the tube pass of the raw material gas cooler is 10-20 ℃;
step 6: heating the liquid phase at the bottom in the methanol desorption tower through a methanol cooler pipe and pressurizing the liquid phase by a methanol pump, and then sending the liquid phase into a methanol regeneration tower; the gas phase in the methanol regeneration tower enters an acid gas treatment device through a tower top gas phase outlet of the methanol regeneration tower to be treated by acid gas; the poor methanol liquid in the methanol regeneration tower is sent into a poor methanol tank through a poor methanol cooler; the poor methanol cooler adopts a circulating water cooling mode;
and 7: pressurizing the poor methanol liquid in the poor methanol tank through a poor methanol pump, cooling the shell pass of a methanol cooler, and then sending the poor methanol liquid into a methanol washing tower from an inlet of a poor methanol spray pipeline for spraying; the pressure of the lean methanol liquid at the outlet of the lean methanol pump is as follows: 5.0-7.5 MPa; the temperature of the poor methanol liquid at the shell pass outlet of the methanol cooler is as follows: -55 ℃ to-62 ℃.
Preferably, the number of the regenerated molecular sieves in the step 2 is two, and the regenerated molecular sieves are in a mutually prepared state;
while the first regenerated molecular sieve is in the adsorption state, the second regenerated molecular sieve is in the regeneration state;
while the second regenerated molecular sieve is in the adsorption state, the first regenerated molecular sieve is in the regeneration state;
when the regenerated molecular sieve is in an adsorption state, the first valve and the second valve are in an open state, and the third valve and the fourth valve are in a closed state; the raw material gas enters the regenerated molecular sieve for adsorption through a first valve, and the adsorbed raw material gas is discharged out of the regenerated molecular sieve through a second valve;
when the regenerated molecular sieve is in a regeneration state, the third valve and the fourth valve are in an opening state, and the first valve and the second valve are in a closing state; and nitrogen in the molecular sieve regenerated gas storage tank enters the regenerated molecular sieve through the fourth valve for regeneration, and the regenerated nitrogen enters the molecular sieve regenerated gas outlet system through the third valve.
According to the anhydrous low-temperature methanol washing device and the production method manufactured according to the scheme, the raw material gas dehydration unit is arranged to remove water from the raw material gas, and the poor methanol liquid is sprayed in the methanol washing tower, so that the water content in the poor methanol/rich methanol/circulating methanol in the whole system is less than 0.01 percent, the device can avoid corrosion of related equipment, save the cost investment of the raw material gas methanol spraying device and the methanol-water separation tower, save the separation of methanol and water in the subsequent process and effectively save the operation cost; furthermore, the invention effectively separates the water in the feed gas by a combined mode of cooling separation and regeneration of the molecular sieve component, thereby preventing the water from entering a subsequent system; has the advantages of simple structure, reasonable design, simple flow, simple and convenient operation and control and intrinsic safety.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
FIG. 2 is a schematic diagram of the structure of a regenerated molecular sieve assembly of the present invention.
In the upper diagram: 1. a feed gas pipeline; 2. a precooler; 3. a water separation tank; 4. a condensate recovery tank; 5. a first valve; 6. a first tee joint; 7. regenerating the molecular sieve; 8. a third valve; 9. a second valve; 10. a second tee joint; 11. a raw gas cooler; 12. a methanol washing tower; 13. a purification gas pipe network; 14. a medium pressure flash column; 15. a methanol desorption tower; 16. a methanol cooler; 17. a methanol pump; 18. a methanol regeneration tower; 19. an acid gas treatment device; 20. a lean methanol cooler; 21. a lean methanol tank; 22. a lean methanol pump; 23. a recycle gas compressor; 24. a resolution gas pipe network; 25. a molecular sieve regeneration gas storage tank; 26. a fourth valve; 27. an inlet of a poor methanol spray pipeline; 28. molecular sieve regeneration gas outlet system.
Detailed Description
In order to more clearly understand the technical features, objects, and effects of the present invention, embodiments of the present invention will now be described with reference to the accompanying drawings, in which like reference numerals refer to like parts throughout. For the sake of simplicity, only the parts relevant to the invention are schematically shown in the drawings, and they do not represent the actual structure as a product.
As shown in fig. 1 and 2, the present invention relates to a waterless low-temperature methanol washing apparatus and a production method thereof, wherein the waterless low-temperature methanol washing apparatus comprises a raw material gas pipeline 1 and a methanol washing tower 12, the raw material gas pipeline 1 is connected with a raw material gas inlet of the methanol washing tower 12 through a raw material gas dehydration unit, and the top of the methanol washing tower 12 is connected with a purification gas pipe network 13; the liquid phase outlet at the bottom of the methanol washing tower 12 is connected with the poor methanol spray pipeline inlet 27 at the middle upper part of the methanol washing tower 12 through a rich methanol treatment unit.
Further, the feed gas dehydration unit comprises at least one dehydration section; in the case of a plurality of dewatering units, the plurality of dewatering units are connected in series.
Further, the dehydration part comprises a precooler 2 and a water separation tank 3 connected with the precooler 2, and a condensate recovery tank 4 is arranged at the bottom of the water separation tank 3.
Further, the dewatering section includes at least one regenerated molecular sieve assembly, and when there are a plurality of regenerated molecular sieve assemblies, the plurality of regenerated molecular sieve assemblies are connected in parallel.
Further, the regenerated molecular sieve component comprises a regenerated molecular sieve 7, the bottom of which is connected with a feed gas pipeline through a first tee joint 6 and a first valve 5, the top of the regenerated molecular sieve 7 is connected with an air outlet pipeline through a second tee joint 10 and a second valve 9, the first tee joint 6 is connected with a molecular sieve regenerated air outlet system 28 through a third valve 8, and the second tee joint 10 is connected with a molecular sieve regenerated air storage tank 25 through a fourth valve 26.
Further, the raw material gas dehydration unit comprises a precooler 2 connected with a raw material gas pipeline 1, an outlet of the precooler 2 is connected with a regenerated molecular sieve 7 through a water separation tank 3, a first valve 5 and a first tee joint 6, and an outlet of the regenerated molecular sieve 7 is connected with a raw material gas inlet of a methanol washing tower 12 through a second tee joint 10, a second valve 9 and a shell pass of a raw material gas cooler 11; the number of the regenerated molecular sieve components is two.
Further, the methanol-rich treatment unit comprises a medium-pressure flash tower 14 connected with a liquid phase outlet at the bottom of the methanol washing tower 12, the liquid phase outlet at the bottom of the medium-pressure flash tower 14 is connected with a methanol analysis tower 15, the liquid phase outlet at the bottom of the methanol analysis tower 15 is connected with a methanol regeneration tower 18 through a methanol cooler 16 tube pass and a methanol pump 17, and the liquid phase outlet at the bottom of the methanol regeneration tower 18 is connected with a poor methanol spray pipeline inlet 27 through a poor methanol cooler 20, a poor methanol tank 21, a poor methanol pump 22 and a methanol cooler 16 shell pass.
Further, a gas phase outlet at the top of the medium-pressure flash tower 14 is connected with a shell side inlet of the raw material gas cooler 11 through a circulating gas compressor 23; a gas phase outlet at the top of the methanol desorption tower 15 is connected with a desorption gas pipe network 24 through a raw gas cooler 11 pipe side; the top gas phase outlet of the methanol regeneration tower 18 is connected with an acid gas treatment device 19.
A production method of an anhydrous low-temperature methanol washing device comprises the following steps:
step 1: the raw material gas in the raw material gas pipeline 1 is cooled by a precooler 2 and then enters a water separation tank 3 for gas-liquid separation, and the liquid phase after the gas-liquid separation enters a condensate recovery device 4; the temperature of the feed gas is as follows: 30-40 ℃, pressure: 4.0-6.5MPa, and the mole fraction of water is 0.1% -0.2%; the temperature of the feed gas at the outlet of the precooler 2 is as follows: the cold source of the precooler 2 is lithium bromide or ammonia at 5-10 ℃;
step 2: the raw material gas after gas-liquid separation enters a regenerated molecular sieve 7 through a first valve 5 for re-dehydration, and the re-dehydrated raw material gas enters the shell pass of a raw material gas cooler 11 through a second tee joint 10 and a second valve 9; the water content in the feed gas passing through the outlet of the regenerated molecular sieve 7 is less than 1 ppm;
and step 3: the raw material gas passing through the shell pass of the raw material gas cooler 11 is cooled and then enters the methanol washing tower 12, the poor methanol entering from the poor methanol spray pipeline inlet 27 is sprayed, the sprayed gas phase enters the purified gas pipe network 13, and the methanol-rich liquid at the bottom of the methanol washing tower 12 enters the medium-pressure flash tower 14 through the liquid phase outlet at the bottom of the methanol washing tower 12; the temperature of the raw material gas at the shell pass outlet of the raw material gas cooler 11 is as follows: -10 to-20 ℃;
and 4, step 4: the methanol-rich liquid solution enters a medium-pressure flash tower 14 to undergo medium-pressure flash evaporation, and vapor after the medium-pressure flash evaporation is pressurized by a circulating gas compressor 23 and then returns to the shell pass of the raw material gas cooler 11 to repeat the step 3; the liquid phase after medium-pressure flash evaporation enters a methanol desorption tower 15; the flash pressure of the medium pressure flash column 14 is: 1.2-1.7 MPa; the circulating gas compressor 23 is a multi-stage centrifugal compressor with an interstage circulating water cooler, and the temperature of flash steam at the outlet of the circulating gas compressor 23 is 20-40 ℃;
and 5: the liquid phase after medium-pressure flash evaporation enters a methanol analysis tower 15 for analysis, and the gas phase enters a raw material gas cooler 11 tube side through a gas phase outlet at the top of the methanol analysis tower 15 for heat exchange with raw material gas of a shell side thereof and then enters an analysis gas pipe network 24; the pressure at the bottom of the 15-column of the methanol desorption tower is 0.05-0.3 MPa; the temperature of the analyzed gas passing through the tube pass of the raw material gas cooler 11 is 10-20 ℃;
step 6: the liquid phase at the bottom in the methanol analysis tower 15 is heated by a methanol cooler 16 tube pass and pressurized by a methanol pump 17 and then sent into a methanol regeneration tower 18; the gas phase in the methanol regeneration tower 18 enters an acid gas treatment device 19 through a tower top gas phase outlet of the methanol regeneration tower 18 for acid gas treatment; the poor methanol liquid in the methanol regeneration tower 18 is sent into a poor methanol tank 21 through a poor methanol cooler 20; the poor methanol cooler 20 adopts a circulating water cooling mode;
and 7: the poor methanol liquid in the poor methanol tank 21 is pressurized by a poor methanol pump 22 and cooled by a methanol cooler 16 shell pass, and then is sent into a methanol washing tower 12 for spraying through a poor methanol spraying pipeline inlet 27; the pressure of the lean methanol liquid at the outlet of the lean methanol pump 22 is: 5.0-7.5 MPa; the temperature of the methanol-poor liquid at the 16-shell-side outlet of the methanol cooler is as follows: -55 ℃ to-62 ℃.
Further, the number of the regenerated molecular sieves 7 in the step 2 is two, and the regenerated molecular sieves are in a mutually standby state;
while the first regenerated molecular sieve 7 is in the adsorption state, the second regenerated molecular sieve 7 is in the regeneration state;
while the second regenerated molecular sieve 7 is in the adsorption state, the first regenerated molecular sieve 7 is in the regeneration state;
when the regenerated molecular sieve 7 is in an adsorption state, the first valve 5 and the second valve 9 are in an open state, and the third valve 8 and the fourth valve 26 are in a closed state; raw material gas enters a regenerated molecular sieve 7 from a first valve 5 for adsorption, and the adsorbed raw material gas is discharged out of the regenerated molecular sieve 7 through a second valve 9;
when the regenerated molecular sieve 7 is in a regeneration state, the third valve 8 and the fourth valve 26 are in an opening state, and the first valve 5 and the second valve 9 are in a closing state; the nitrogen in the molecular sieve regeneration gas storage tank 25 enters the regenerated molecular sieve 7 through the fourth valve 26 for regeneration, and the regenerated nitrogen enters the molecular sieve regeneration gas outlet system 28 through the third valve 8.
The present invention will now be further illustrated with reference to examples in order to explain the present invention in more detail. The specific embodiment is as follows:
example 1
A non-water type low-temperature methanol washing device comprises a raw material gas pipeline 1 and a methanol washing tower 12, wherein the raw material gas pipeline 1 is connected with a raw material gas inlet of the methanol washing tower 12 through a raw material gas dehydration unit, and the top of the methanol washing tower 12 is connected with a purified gas pipe network 13; the liquid phase outlet at the bottom of the methanol washing tower 12 is connected with the poor methanol spray pipeline inlet 27 at the middle upper part of the methanol washing tower 12 through a rich methanol treatment unit. The raw material gas dehydration unit comprises a dehydration part; the dehydration part comprises a precooler 2 and a water separation tank 3 connected with the precooler 2, and the bottom of the water separation tank 3 is provided with a condensate recovery tank 4. The methanol-rich treatment unit comprises a medium-pressure flash tower 14 connected with a liquid phase outlet at the bottom of a methanol washing tower 12, the liquid phase outlet at the bottom of the medium-pressure flash tower 14 is connected with a methanol analysis tower 15, the liquid phase outlet at the bottom of the methanol analysis tower 15 is connected with a methanol regeneration tower 18 through a methanol cooler 16 tube pass and a methanol pump 17, and the liquid phase outlet at the bottom of the methanol regeneration tower 18 is connected with a poor methanol spray pipeline inlet 27 through a poor methanol cooler 20, a poor methanol tank 21, a poor methanol pump 22 and a methanol cooler 16 shell pass. A gas phase outlet at the top of the medium-pressure flash tower 14 is connected with a shell pass inlet of the raw material gas cooler 11 through a circulating gas compressor 23; a gas phase outlet at the top of the methanol desorption tower 15 is connected with a desorption gas pipe network 24 through a raw gas cooler 11 pipe side; the top gas phase outlet of the methanol regeneration tower 18 is connected with an acid gas treatment device 19.
Example 2
A non-water type low-temperature methanol washing device comprises a raw material gas pipeline 1 and a methanol washing tower 12, wherein the raw material gas pipeline 1 is connected with a raw material gas inlet of the methanol washing tower 12 through a raw material gas dehydration unit, and the top of the methanol washing tower 12 is connected with a purified gas pipe network 13; the liquid phase outlet at the bottom of the methanol washing tower 12 is connected with the poor methanol spray pipeline inlet 27 at the middle upper part of the methanol washing tower 12 through a rich methanol treatment unit. The raw material gas dehydration unit comprises two dehydration parts; the two dehydration parts are connected in series; the two dewatering parts are both in a cooling dewatering form, namely the dewatering parts comprise a precooler 2 and a water separation tank 3 connected with the precooler 2, and the bottom of the water separation tank 3 is provided with a condensate recovery tank 4. The methanol-rich treatment unit comprises a medium-pressure flash tower 14 connected with a liquid phase outlet at the bottom of a methanol washing tower 12, the liquid phase outlet at the bottom of the medium-pressure flash tower 14 is connected with a methanol analysis tower 15, the liquid phase outlet at the bottom of the methanol analysis tower 15 is connected with a methanol regeneration tower 18 through a methanol cooler 16 tube pass and a methanol pump 17, and the liquid phase outlet at the bottom of the methanol regeneration tower 18 is connected with a poor methanol spray pipeline inlet 27 through a poor methanol cooler 20, a poor methanol tank 21, a poor methanol pump 22 and a methanol cooler 16 shell pass. A gas phase outlet at the top of the medium-pressure flash tower 14 is connected with a shell pass inlet of the raw material gas cooler 11 through a circulating gas compressor 23; a gas phase outlet at the top of the methanol desorption tower 15 is connected with a desorption gas pipe network 24 through a raw gas cooler 11 pipe side; the top gas phase outlet of the methanol regeneration tower 18 is connected with an acid gas treatment device 19.
Example 3
A non-water type low-temperature methanol washing device comprises a raw material gas pipeline 1 and a methanol washing tower 12, wherein the raw material gas pipeline 1 is connected with a raw material gas inlet of the methanol washing tower 12 through a raw material gas dehydration unit, and the top of the methanol washing tower 12 is connected with a purified gas pipe network 13; the liquid phase outlet at the bottom of the methanol washing tower 12 is connected with the poor methanol spray pipeline inlet 27 at the middle upper part of the methanol washing tower 12 through a rich methanol treatment unit. The raw material gas dehydration unit is a dehydration part; the dewatering section is comprised of a regenerated molecular sieve assembly. The regenerated molecular sieve component comprises a regenerated molecular sieve 7, the bottom of the regenerated molecular sieve is connected with a feed gas pipeline through a first tee joint 6 and a first valve 5, the top of the regenerated molecular sieve 7 is connected with an air outlet pipeline through a second tee joint 10 and a second valve 9, the first tee joint 6 is connected with a molecular sieve regenerated air outlet system 28 through a third valve 8, and the second tee joint 10 is connected with a molecular sieve regenerated air storage tank 25 through a fourth valve 26. The feed gas dehydration unit comprises a precooler 2 connected with a feed gas pipeline 1, the outlet of the precooler 2 is connected with a regenerated molecular sieve 7 through a water separation tank 3, a first valve 5 and a first tee joint 6, and the outlet of the regenerated molecular sieve 7 is connected with the feed gas inlet of a methanol washing tower 12 through a second tee joint 10, a second valve 9 and the shell pass of a feed gas cooler 11. The methanol-rich treatment unit comprises a medium-pressure flash tower 14 connected with a liquid phase outlet at the bottom of a methanol washing tower 12, the liquid phase outlet at the bottom of the medium-pressure flash tower 14 is connected with a methanol analysis tower 15, the liquid phase outlet at the bottom of the methanol analysis tower 15 is connected with a methanol regeneration tower 18 through a methanol cooler 16 tube pass and a methanol pump 17, and the liquid phase outlet at the bottom of the methanol regeneration tower 18 is connected with a poor methanol spray pipeline inlet 27 through a poor methanol cooler 20, a poor methanol tank 21, a poor methanol pump 22 and a methanol cooler 16 shell pass. A gas phase outlet at the top of the medium-pressure flash tower 14 is connected with a shell pass inlet of the raw material gas cooler 11 through a circulating gas compressor 23; a gas phase outlet at the top of the methanol desorption tower 15 is connected with a desorption gas pipe network 24 through a raw gas cooler 11 pipe side; the top gas phase outlet of the methanol regeneration tower 18 is connected with an acid gas treatment device 19.
Example 4
A non-water type low-temperature methanol washing device comprises a raw material gas pipeline 1 and a methanol washing tower 12, wherein the raw material gas pipeline 1 is connected with a raw material gas inlet of the methanol washing tower 12 through a raw material gas dehydration unit, and the top of the methanol washing tower 12 is connected with a purified gas pipe network 13; the liquid phase outlet at the bottom of the methanol washing tower 12 is connected with the poor methanol spray pipeline inlet 27 at the middle upper part of the methanol washing tower 12 through a rich methanol treatment unit. The raw material gas dehydration unit comprises two dehydration parts; the two dehydration parts are both in a regenerated molecular sieve dehydration form and are connected in series. The dehydration part comprises two regenerated molecular sieve components which are connected in parallel. The regenerated molecular sieve component comprises a regenerated molecular sieve 7, the bottom of the regenerated molecular sieve is connected with a feed gas pipeline through a first tee joint 6 and a first valve 5, the top of the regenerated molecular sieve 7 is connected with an air outlet pipeline through a second tee joint 10 and a second valve 9, the first tee joint 6 is connected with a molecular sieve regenerated air outlet system 28 through a third valve 8, and the second tee joint 10 is connected with a molecular sieve regenerated air storage tank 25 through a fourth valve 26. The feed gas dehydration unit comprises a precooler 2 connected with a feed gas pipeline 1, the outlet of the precooler 2 is connected with a regenerated molecular sieve 7 through a water separation tank 3, a first valve 5 and a first tee joint 6, and the outlet of the regenerated molecular sieve 7 is connected with the feed gas inlet of a methanol washing tower 12 through a second tee joint 10, a second valve 9 and the shell pass of a feed gas cooler 11; the number of the regenerated molecular sieve components is two. The methanol-rich treatment unit comprises a medium-pressure flash tower 14 connected with a liquid phase outlet at the bottom of a methanol washing tower 12, the liquid phase outlet at the bottom of the medium-pressure flash tower 14 is connected with a methanol analysis tower 15, the liquid phase outlet at the bottom of the methanol analysis tower 15 is connected with a methanol regeneration tower 18 through a methanol cooler 16 tube pass and a methanol pump 17, and the liquid phase outlet at the bottom of the methanol regeneration tower 18 is connected with a poor methanol spray pipeline inlet 27 through a poor methanol cooler 20, a poor methanol tank 21, a poor methanol pump 22 and a methanol cooler 16 shell pass. A gas phase outlet at the top of the medium-pressure flash tower 14 is connected with a shell pass inlet of the raw material gas cooler 11 through a circulating gas compressor 23; a gas phase outlet at the top of the methanol desorption tower 15 is connected with a desorption gas pipe network 24 through a raw gas cooler 11 pipe side; the top gas phase outlet of the methanol regeneration tower 18 is connected with an acid gas treatment device 19.
Example 5
A non-water type low-temperature methanol washing device comprises a raw material gas pipeline 1 and a methanol washing tower 12, wherein the raw material gas pipeline 1 is connected with a raw material gas inlet of the methanol washing tower 12 through a raw material gas dehydration unit, and the top of the methanol washing tower 12 is connected with a purified gas pipe network 13; the liquid phase outlet at the bottom of the methanol washing tower 12 is connected with the poor methanol spray pipeline inlet 27 at the middle upper part of the methanol washing tower 12 through a rich methanol treatment unit. The raw material gas dehydration unit comprises two dehydration parts; the two dehydration parts are connected in series, the front dehydration part is in a cooling dehydration form, and the rear dehydration part is in a regenerated molecular sieve dehydration form. The front dehydration part comprises a precooler 2 and a water separation tank 3 connected with the precooler 2, and the bottom of the water separation tank 3 is provided with a condensate recovery tank 4. The back dehydration portion is including being a regeneration molecular sieve subassembly, regeneration molecular sieve subassembly includes that regeneration molecular sieve 7's bottom links to each other with the feed gas pipeline through first tee bend 6 and first valve 5, and regeneration molecular sieve 7's top is passed through second tee bend 10 and second valve 9 and is linked to each other with the pipeline of giving vent to anger, and first tee bend 6 links to each other with molecular sieve regeneration gas outlet system 28 through third valve 8, and second tee bend 10 is passed through fourth valve 26 and is linked to each other with molecular sieve regeneration gas storage tank 25. The feed gas dehydration unit comprises a precooler 2 connected with a feed gas pipeline 1, the outlet of the precooler 2 is connected with a regenerated molecular sieve 7 through a water separation tank 3, a first valve 5 and a first tee joint 6, and the outlet of the regenerated molecular sieve 7 is connected with the feed gas inlet of a methanol washing tower 12 through a second tee joint 10, a second valve 9 and the shell pass of a feed gas cooler 11. The methanol-rich treatment unit comprises a medium-pressure flash tower 14 connected with a liquid phase outlet at the bottom of a methanol washing tower 12, the liquid phase outlet at the bottom of the medium-pressure flash tower 14 is connected with a methanol analysis tower 15, the liquid phase outlet at the bottom of the methanol analysis tower 15 is connected with a methanol regeneration tower 18 through a methanol cooler 16 tube pass and a methanol pump 17, and the liquid phase outlet at the bottom of the methanol regeneration tower 18 is connected with a poor methanol spray pipeline inlet 27 through a poor methanol cooler 20, a poor methanol tank 21, a poor methanol pump 22 and a methanol cooler 16 shell pass. A gas phase outlet at the top of the medium-pressure flash tower 14 is connected with a shell pass inlet of the raw material gas cooler 11 through a circulating gas compressor 23; a gas phase outlet at the top of the methanol desorption tower 15 is connected with a desorption gas pipe network 24 through a raw gas cooler 11 pipe side; the top gas phase outlet of the methanol regeneration tower 18 is connected with an acid gas treatment device 19.
Example 6
A non-water type low-temperature methanol washing device comprises a raw material gas pipeline 1 and a methanol washing tower 12, wherein the raw material gas pipeline 1 is connected with a raw material gas inlet of the methanol washing tower 12 through a raw material gas dehydration unit, and the top of the methanol washing tower 12 is connected with a purified gas pipe network 13; the liquid phase outlet at the bottom of the methanol washing tower 12 is connected with the poor methanol spray pipeline inlet 27 at the middle upper part of the methanol washing tower 12 through a rich methanol treatment unit. The raw material gas dehydration unit comprises two dehydration parts; the two dehydration parts are connected in series, the front dehydration part is in a cooling dehydration form, and the rear dehydration part is in a regenerated molecular sieve dehydration form. The front dehydration part comprises a precooler 2 and a water separation tank 3 connected with the precooler 2, and the bottom of the water separation tank 3 is provided with a condensate recovery tank 4. The post-dehydration part comprises two regenerated molecular sieve components which are connected in parallel. The regenerated molecular sieve component comprises a regenerated molecular sieve 7, the bottom of the regenerated molecular sieve is connected with a feed gas pipeline through a first tee joint 6 and a first valve 5, the top of the regenerated molecular sieve 7 is connected with an air outlet pipeline through a second tee joint 10 and a second valve 9, the first tee joint 6 is connected with a molecular sieve regenerated air outlet system 28 through a third valve 8, and the second tee joint 10 is connected with a molecular sieve regenerated air storage tank 25 through a fourth valve 26. The feed gas dehydration unit comprises a precooler 2 connected with a feed gas pipeline 1, the outlet of the precooler 2 is connected with a regenerated molecular sieve 7 through a water separation tank 3, a first valve 5 and a first tee joint 6, and the outlet of the regenerated molecular sieve 7 is connected with the feed gas inlet of a methanol washing tower 12 through a second tee joint 10, a second valve 9 and the shell pass of a feed gas cooler 11. The methanol-rich treatment unit comprises a medium-pressure flash tower 14 connected with a liquid phase outlet at the bottom of a methanol washing tower 12, the liquid phase outlet at the bottom of the medium-pressure flash tower 14 is connected with a methanol analysis tower 15, the liquid phase outlet at the bottom of the methanol analysis tower 15 is connected with a methanol regeneration tower 18 through a methanol cooler 16 tube pass and a methanol pump 17, and the liquid phase outlet at the bottom of the methanol regeneration tower 18 is connected with a poor methanol spray pipeline inlet 27 through a poor methanol cooler 20, a poor methanol tank 21, a poor methanol pump 22 and a methanol cooler 16 shell pass. A gas phase outlet at the top of the medium-pressure flash tower 14 is connected with a shell pass inlet of the raw material gas cooler 11 through a circulating gas compressor 23; a gas phase outlet at the top of the methanol desorption tower 15 is connected with a desorption gas pipe network 24 through a raw gas cooler 11 pipe side; the top gas phase outlet of the methanol regeneration tower 18 is connected with an acid gas treatment device 19.
Example 7
The production method of the anhydrous low-temperature methanol washing device in the structural form of the embodiment 5 comprises the following steps:
step 1: the raw material gas in the raw material gas pipeline 1 is cooled by a precooler 2 and then enters a water separation tank 3 for gas-liquid separation, and the liquid phase after the gas-liquid separation enters a condensate recovery device 4; the temperature of the feed gas is as follows: 30-40 ℃, pressure: 4.0-6.5MPa, and the mole fraction of water is 0.1% -0.2%; the temperature of the feed gas at the outlet of the precooler 2 is as follows: the cold source of the precooler 2 is lithium bromide at the temperature of 5-10 ℃;
step 2: the raw material gas after gas-liquid separation enters a regenerated molecular sieve 7 through a first valve 5 for re-dehydration, and the re-dehydrated raw material gas enters the shell pass of a raw material gas cooler 11 through a second tee joint 10 and a second valve 9; the water content in the feed gas passing through the outlet of the regenerated molecular sieve 7 is 0.8 ppm;
and step 3: the raw material gas passing through the shell pass of the raw material gas cooler 11 is cooled and then enters the methanol washing tower 12, the poor methanol entering from the poor methanol spray pipeline inlet 27 is sprayed, the sprayed gas phase enters the purified gas pipe network 13, and the methanol-rich liquid at the bottom of the methanol washing tower 12 enters the medium-pressure flash tower 14 through the liquid phase outlet at the bottom of the methanol washing tower 12; the temperature of the raw material gas at the shell pass outlet of the raw material gas cooler 11 is as follows: -10 to-20 ℃;
and 4, step 4: the methanol-rich liquid solution enters a medium-pressure flash tower 14 to undergo medium-pressure flash evaporation, and vapor after the medium-pressure flash evaporation is pressurized by a circulating gas compressor 23 and then returns to the shell pass of the raw material gas cooler 11 to repeat the step 3; the liquid phase after medium-pressure flash evaporation enters a methanol desorption tower 15; the flash pressure of the medium pressure flash column 14 is: 1.2-1.7 MPa; the circulating gas compressor 23 is a multi-stage centrifugal compressor with an interstage circulating water cooler, and the temperature of flash steam at the outlet of the circulating gas compressor 23 is 20-40 ℃;
and 5: the liquid phase after medium-pressure flash evaporation enters a methanol analysis tower 15 for analysis, and the gas phase enters a raw material gas cooler 11 tube side through a gas phase outlet at the top of the methanol analysis tower 15 for heat exchange with raw material gas of a shell side thereof and then enters an analysis gas pipe network 24; the pressure at the bottom of the 15-column of the methanol desorption tower is 0.05-0.3 MPa; the temperature of the analyzed gas passing through the tube pass of the raw material gas cooler 11 is 10-20 ℃;
step 6: the liquid phase at the bottom in the methanol analysis tower 15 is heated by a methanol cooler 16 tube pass and pressurized by a methanol pump 17 and then sent into a methanol regeneration tower 18; the gas phase in the methanol regeneration tower 18 enters an acid gas treatment device 19 through a tower top gas phase outlet of the methanol regeneration tower 18 for acid gas treatment; the poor methanol liquid in the methanol regeneration tower 18 is sent into a poor methanol tank 21 through a poor methanol cooler 20; the poor methanol cooler 20 adopts a circulating water cooling mode;
and 7: the poor methanol liquid in the poor methanol tank 21 is pressurized by a poor methanol pump 22 and cooled by a methanol cooler 16 shell pass, and then is sent into a methanol washing tower 12 for spraying through a poor methanol spraying pipeline inlet 27; the pressure of the lean methanol liquid at the outlet of the lean methanol pump 22 is: 5.0-7.5 MPa; the temperature of the methanol-poor liquid at the 16-shell-side outlet of the methanol cooler is as follows: -55 ℃ to-62 ℃.
Example 8
The production method of the anhydrous low-temperature methanol washing device in the structural form of the embodiment 6 comprises the following steps:
step 1: the raw material gas in the raw material gas pipeline 1 is cooled by a precooler 2 and then enters a water separation tank 3 for gas-liquid separation, and the liquid phase after the gas-liquid separation enters a condensate recovery device 4; the temperature of the feed gas is as follows: 30-40 ℃, pressure: 4.0-6.5MPa, and the mole fraction of water is 0.1% -0.2%; the temperature of the feed gas at the outlet of the precooler 2 is as follows: the cold source of the precooler 2 is ammonia cold at 5-10 ℃;
step 2: the raw material gas after gas-liquid separation enters a regenerated molecular sieve 7 through a first valve 5 for re-dehydration, and the re-dehydrated raw material gas enters the shell pass of a raw material gas cooler 11 through a second tee joint 10 and a second valve 9; the water content in the feed gas passing through the outlet of the regenerated molecular sieve 7 is 0.6 ppm;
and step 3: the raw material gas passing through the shell pass of the raw material gas cooler 11 is cooled and then enters the methanol washing tower 12, the poor methanol entering from the poor methanol spray pipeline inlet 27 is sprayed, the sprayed gas phase enters the purified gas pipe network 13, and the methanol-rich liquid at the bottom of the methanol washing tower 12 enters the medium-pressure flash tower 14 through the liquid phase outlet at the bottom of the methanol washing tower 12; the temperature of the raw material gas at the shell pass outlet of the raw material gas cooler 11 is as follows: -10 to-20 ℃;
and 4, step 4: the methanol-rich liquid solution enters a medium-pressure flash tower 14 to undergo medium-pressure flash evaporation, and vapor after the medium-pressure flash evaporation is pressurized by a circulating gas compressor 23 and then returns to the shell pass of the raw material gas cooler 11 to repeat the step 3; the liquid phase after medium-pressure flash evaporation enters a methanol desorption tower 15; the flash pressure of the medium pressure flash column 14 is: 1.2-1.7 MPa; the circulating gas compressor 23 is a multi-stage centrifugal compressor with an interstage circulating water cooler, and the temperature of flash steam at the outlet of the circulating gas compressor 23 is 20-40 ℃;
and 5: the liquid phase after medium-pressure flash evaporation enters a methanol analysis tower 15 for analysis, and the gas phase enters a raw material gas cooler 11 tube side through a gas phase outlet at the top of the methanol analysis tower 15 for heat exchange with raw material gas of a shell side thereof and then enters an analysis gas pipe network 24; the pressure at the bottom of the 15-column of the methanol desorption tower is 0.05-0.3 MPa; the temperature of the analyzed gas passing through the tube pass of the raw material gas cooler 11 is 10-20 ℃;
step 6: the liquid phase at the bottom in the methanol analysis tower 15 is heated by a methanol cooler 16 tube pass and pressurized by a methanol pump 17 and then sent into a methanol regeneration tower 18; the gas phase in the methanol regeneration tower 18 enters an acid gas treatment device 19 through a tower top gas phase outlet of the methanol regeneration tower 18 for acid gas treatment; the poor methanol liquid in the methanol regeneration tower 18 is sent into a poor methanol tank 21 through a poor methanol cooler 20; the poor methanol cooler 20 adopts a circulating water cooling mode;
and 7: the poor methanol liquid in the poor methanol tank 21 is pressurized by a poor methanol pump 22 and cooled by a methanol cooler 16 shell pass, and then is sent into a methanol washing tower 12 for spraying through a poor methanol spraying pipeline inlet 27; the pressure of the lean methanol liquid at the outlet of the lean methanol pump 22 is: 5.0-7.5 MPa; the temperature of the methanol-poor liquid at the 16-shell-side outlet of the methanol cooler is as follows: -55 to-62 ℃.
Further, the number of the regenerated molecular sieves 7 in the step 2 is two, and the regenerated molecular sieves are in a mutually standby state;
while the first regenerated molecular sieve 7 is in the adsorption state, the second regenerated molecular sieve 7 is in the regeneration state;
while the second regenerated molecular sieve 7 is in the adsorption state, the first regenerated molecular sieve 7 is in the regeneration state;
when the regenerated molecular sieve 7 is in an adsorption state, the first valve 5 and the second valve 9 are in an open state, and the third valve 8 and the fourth valve 26 are in a closed state; raw material gas enters a regenerated molecular sieve 7 from a first valve 5 for adsorption, and the adsorbed raw material gas is discharged out of the regenerated molecular sieve 7 through a second valve 9;
when the regenerated molecular sieve 7 is in a regeneration state, the third valve 8 and the fourth valve 26 are in an opening state, and the first valve 5 and the second valve 9 are in a closing state; the nitrogen in the molecular sieve regeneration gas storage tank 25 enters the regenerated molecular sieve 7 through the fourth valve 26 for regeneration, and the regenerated nitrogen enters the molecular sieve regeneration gas outlet system 28 through the third valve 8.
Example 9
The production method of the anhydrous low-temperature methanol washing device in the structural form of the embodiment 6 comprises the following steps:
step 1: the raw material gas in the raw material gas pipeline 1 is cooled by a precooler 2 and then enters a water separation tank 3 for gas-liquid separation, and the liquid phase after the gas-liquid separation enters a condensate recovery device 4; the temperature of the feed gas is as follows: 30-40 ℃, pressure: 4.0-6.5MPa, and the mole fraction of water is 0.1% -0.2%; the temperature of the feed gas at the outlet of the precooler 2 is as follows: the cold source of the precooler 2 is lithium bromide at the temperature of 5-10 ℃;
step 2: the raw material gas after gas-liquid separation enters a regenerated molecular sieve 7 through a first valve 5 for re-dehydration, and the re-dehydrated raw material gas enters the shell pass of a raw material gas cooler 11 through a second tee joint 10 and a second valve 9; the water content in the feed gas passing through the outlet of the regenerated molecular sieve 7 is 0.7 ppm;
and step 3: the raw material gas passing through the shell pass of the raw material gas cooler 11 is cooled and then enters the methanol washing tower 12, the poor methanol entering from the poor methanol spray pipeline inlet 27 is sprayed, the sprayed gas phase enters the purified gas pipe network 13, and the methanol-rich liquid at the bottom of the methanol washing tower 12 enters the medium-pressure flash tower 14 through the liquid phase outlet at the bottom of the methanol washing tower 12; the temperature of the raw material gas at the shell pass outlet of the raw material gas cooler 11 is as follows: -10 to-20 ℃;
and 4, step 4: the methanol-rich liquid solution enters a medium-pressure flash tower 14 to undergo medium-pressure flash evaporation, and vapor after the medium-pressure flash evaporation is pressurized by a circulating gas compressor 23 and then returns to the shell pass of the raw material gas cooler 11 to repeat the step 3; the liquid phase after medium-pressure flash evaporation enters a methanol desorption tower 15; the flash pressure of the medium pressure flash column 14 is: 1.2-1.7 MPa; the circulating gas compressor 23 is a multi-stage centrifugal compressor with an interstage circulating water cooler, and the temperature of flash steam at the outlet of the circulating gas compressor 23 is 20-40 ℃;
and 5: the liquid phase after medium-pressure flash evaporation enters a methanol analysis tower 15 for analysis, and the gas phase enters a raw material gas cooler 11 tube side through a gas phase outlet at the top of the methanol analysis tower 15 for heat exchange with raw material gas of a shell side thereof and then enters an analysis gas pipe network 24; the pressure at the bottom of the 15-column of the methanol desorption tower is 0.05-0.3 MPa; the temperature of the analyzed gas passing through the tube pass of the raw material gas cooler 11 is 10-20 ℃;
step 6: the liquid phase at the bottom in the methanol analysis tower 15 is heated by a methanol cooler 16 tube pass and pressurized by a methanol pump 17 and then sent into a methanol regeneration tower 18; the gas phase in the methanol regeneration tower 18 enters an acid gas treatment device 19 through a tower top gas phase outlet of the methanol regeneration tower 18 for acid gas treatment; the poor methanol liquid in the methanol regeneration tower 18 is sent into a poor methanol tank 21 through a poor methanol cooler 20; the poor methanol cooler 20 adopts a circulating water cooling mode;
and 7: the poor methanol liquid in the poor methanol tank 21 is pressurized by a poor methanol pump 22 and cooled by a methanol cooler 16 shell pass, and then is sent into a methanol washing tower 12 for spraying through a poor methanol spraying pipeline inlet 27; the pressure of the lean methanol liquid at the outlet of the lean methanol pump 22 is: 5.0-7.5 MPa; the temperature of the methanol-poor liquid at the 16-shell-side outlet of the methanol cooler is as follows: -55 to-62 ℃.
Further, the number of the regenerated molecular sieves 7 in the step 2 is two, and the regenerated molecular sieves are in a mutually standby state;
while the first regenerated molecular sieve 7 is in the adsorption state, the second regenerated molecular sieve 7 is in the regeneration state;
while the second regenerated molecular sieve 7 is in the adsorption state, the first regenerated molecular sieve 7 is in the regeneration state;
when the regenerated molecular sieve 7 is in an adsorption state, the first valve 5 and the second valve 9 are in an open state, and the third valve 8 and the fourth valve 26 are in a closed state; raw material gas enters a regenerated molecular sieve 7 from a first valve 5 for adsorption, and the adsorbed raw material gas is discharged out of the regenerated molecular sieve 7 through a second valve 9;
when the regenerated molecular sieve 7 is in a regeneration state, the third valve 8 and the fourth valve 26 are in an opening state, and the first valve 5 and the second valve 9 are in a closing state; the nitrogen in the molecular sieve regeneration gas storage tank 25 enters the regenerated molecular sieve 7 through the fourth valve 26 for regeneration, and the regenerated nitrogen enters the molecular sieve regeneration gas outlet system 28 through the third valve 8.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected," "connecting," and the like are to be construed broadly, and may, for example, be fixedly connected, integrally connected, or detachably connected; or communication between the interior of the two elements; they may be directly connected or indirectly connected through an intermediate, and those skilled in the art can understand the specific meaning of the above terms in the present invention according to specific situations. The above examples are merely illustrative of the feasible embodiments of the present invention and they are not intended to limit the scope of the present invention, and equivalent embodiments, modifications and alterations without departing from the technical spirit of the present invention are included in the scope of the present invention.
Claims (10)
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040065199A1 (en) * | 2002-10-07 | 2004-04-08 | Alexandre Rojey | Natural gas deacidizing method |
| CN203139876U (en) * | 2012-12-26 | 2013-08-21 | 新奥科技发展有限公司 | Low-temperature methanol washing process device |
| CN104098441A (en) * | 2014-06-05 | 2014-10-15 | 上海戊正工程技术有限公司 | Technology and device system for producing dimethyl oxalate by high-pressure carbonylation of industrial synthesis gases and producing ethylene glycol through dimethyl oxalate hydrogenation |
| CN106403499A (en) * | 2016-08-31 | 2017-02-15 | 惠生工程（中国）有限公司 | Method for co-production of high-concentration liquid CO2 by utilizing low-temperature methanol washing process |
| CN210385374U (en) * | 2019-07-29 | 2020-04-24 | 河南心连心化学工业集团股份有限公司 | Acid gas methanol recovery device in low-temperature methanol washing process |
| EP3851179A1 (en) * | 2020-01-14 | 2021-07-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for separating a synthesis gas by cryogenic distillation |
| CN215939524U (en) * | 2021-09-02 | 2022-03-04 | 河南心连心化学工业集团股份有限公司 | Device is washed to anhydrous type low temperature methyl alcohol |
-
2021
- 2021-09-02 CN CN202111027365.XA patent/CN113599978B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040065199A1 (en) * | 2002-10-07 | 2004-04-08 | Alexandre Rojey | Natural gas deacidizing method |
| CN203139876U (en) * | 2012-12-26 | 2013-08-21 | 新奥科技发展有限公司 | Low-temperature methanol washing process device |
| CN104098441A (en) * | 2014-06-05 | 2014-10-15 | 上海戊正工程技术有限公司 | Technology and device system for producing dimethyl oxalate by high-pressure carbonylation of industrial synthesis gases and producing ethylene glycol through dimethyl oxalate hydrogenation |
| CN106403499A (en) * | 2016-08-31 | 2017-02-15 | 惠生工程（中国）有限公司 | Method for co-production of high-concentration liquid CO2 by utilizing low-temperature methanol washing process |
| CN210385374U (en) * | 2019-07-29 | 2020-04-24 | 河南心连心化学工业集团股份有限公司 | Acid gas methanol recovery device in low-temperature methanol washing process |
| EP3851179A1 (en) * | 2020-01-14 | 2021-07-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for separating a synthesis gas by cryogenic distillation |
| CN215939524U (en) * | 2021-09-02 | 2022-03-04 | 河南心连心化学工业集团股份有限公司 | Device is washed to anhydrous type low temperature methyl alcohol |
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