CN216934749U - Energy-conserving flash distillation plant is washed to low temperature methyl alcohol - Google Patents
Energy-conserving flash distillation plant is washed to low temperature methyl alcohol Download PDFInfo
- Publication number
- CN216934749U CN216934749U CN202220168202.7U CN202220168202U CN216934749U CN 216934749 U CN216934749 U CN 216934749U CN 202220168202 U CN202220168202 U CN 202220168202U CN 216934749 U CN216934749 U CN 216934749U
- Authority
- CN
- China
- Prior art keywords
- gas
- sulfur
- methanol
- section
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Landscapes
- Industrial Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The application provides a low temperature methanol washing energy-saving flash distillation device, sets up the three-layer column plate through the sulphur methyl alcohol middling pressure flash distillation section at ordinary pressure low pressure flash distillation tower to the position of each input/output pipeline interface of design, most CO in with the effective gas in the sulphur methyl alcohol middling pressure flash distillation section2The methanol liquid is used for washing and absorbing at the three layers of tower plates, so that the volume of the recovered effective gas is reduced, the energy consumption of the compressor for compressing the effective gas is reduced, meanwhile, the energy consumption of the effective gas recovered by repeated cooling is also reduced, the utilization efficiency of the condensing agent and the cooling separation device is improved, and the device has higher popularization and application values.
Description
Technical Field
The invention relates to the technical field of gas purification devices, in particular to a low-temperature methanol washing energy-saving flash evaporation device.
Background
The low-temperature methanol washing process is a process for removing acid gas from gas jointly developed by Linde and Luqi two companies in the 50 th century in 19 th century, and the principle of the process belongs to physical absorption. The process has the main characteristics of high gas purification degree, good absorption selectivity, and good thermal stability and chemical stability of absorbent methanolCan absorb CO in the gas at the same time2、H2S, COS, HCN, and the like. The process is widely applied to gas purification devices for hydrogen production, ammonia synthesis, methanol synthesis, coal-based natural gas and the like, and the gas purification technology of the existing large-scale coal chemical device also mostly adopts a low-temperature methanol washing process to purify the initial gas.
Liquid CO2The temperature is close to-56.57 ℃, the steam pressure is higher and is 0.518MPa at the lowest, and CO is flashed2The gas has higher kinetic energy and low flash evaporation temperature, and the flash evaporation temperature is lower than that of other refrigerants under the same pressure, and the evaporation temperature at 0.518Mpa can provide refrigeration temperature of about-55 ℃, so that part of CO in the initial gas of almost all coal gasification technologies can be used2Condensing without additional supply of CO in the raw material gas2The cold required for liquefaction.
Patent CN102971253A proposes the separation of CO by liquefaction2The process idea of (1) and separating to obtain liquid CO2Products, but not making full use of liquid CO2Performance as an absorbent. The patent CN104208978B improves the flow of low-temperature methanol washing on the basis of the patent CN102971253A and designs and utilizes liquid CO2Absorbent properties of (a).
In condensing CO2In the process of (3), part of the effective gas in the initial gas, e.g. H2CO is also dissolved in liquid CO2In the prior art, when the partial effective gas is recovered by pressure reduction flash evaporation, more liquid CO exists2The gas phase is changed to enter an effective gas circulation module and repeatedly enters an initial gas cooling and separating device, so that the energy utilization efficiency is reduced and wasted, and the energy consumption of the compressor is obviously increased due to the fact that the amount of the recovered effective gas is large.
Disclosure of Invention
In view of the above defects or shortcomings in the prior art, the present application aims to provide a low-temperature methanol-washing energy-saving flash evaporation device, wherein a tower plate is arranged in a sulfur-containing methanol medium-pressure flash evaporation section of a normal-pressure low-pressure flash evaporation tower, and the positions of the interfaces of the input and output pipelines are designed, so that most of CO in effective gas is washed and absorbed by methanol liquid at the tower plate of the sulfur-containing methanol medium-pressure flash evaporation section2Therefore, the volume of effective gas output by the sulfur-containing methanol medium-pressure flash evaporation section is reduced, the energy consumption of the effective gas recycling module for recycling the effective gas is reduced, the energy consumption of the cooling separation device for repeatedly cooling the effective gas is reduced, and the utilization efficiency of the condensing agent and the cooling separation device is improved.
The application provides a low temperature methanol washing energy-saving flash distillation device, including being used for containing CO2And a medium-low pressure flash column (C2) for the vacuum flash evaporation of the sulphide-rich methanol liquid, characterized in that the medium-low pressure flash column (C2) comprises a reactor for reacting CO2An effective gas recovery section (C2-1) for obtaining an effective gas a by flashing the liquid a under reduced pressure and a method for absorbing CO2A sulfur-containing methanol medium-pressure flash section (C2-2) outputting effective gas C; a tower plate is arranged in the sulfur-containing methanol medium-pressure flash section (C2-2);
the upper part of the effective gas recovery section (C2-1) is provided with a pipeline connected with the sulfur-containing methanol medium-pressure flash section (C2-2), the position of a pipeline joint connected with the sulfur-containing methanol medium-pressure flash section (C2-2) is lower than the tower plate, and the effective gas recovery section is also provided with a pipeline used for condensing and separating CO in the initial gas2Obtaining CO2A pipeline connected with a second liquid output port of the cooling and separating device for the liquid a and the gas a; the sulfur-containing methanol medium-pressure flash evaporation section (C2-2) is provided with a methanol liquid input pipeline, the pipeline interface position is higher than the tower plate, a pipeline connected with an effective gas circulation module is also arranged, the pipeline interface position is higher than the tower plate, and the other end of the effective gas circulation module is connected with the cooling separation device.
According to an embodiment of the application, the cooling separation device comprises a first cooling separation module, liquid CO2An evaporator (E7) and a second cooling and separating module; the liquid CO2The evaporator (E7) comprises a first inlet, a first outlet, a second inlet, a second outlet;
the output end of the first cooling and separating module is connected with the first inlet, and the input end of the first cooling and separating module is connected with an initial gas conveying pipeline; the input end of the second cooling and separating module is connected with the first outlet, the output end of the second cooling and separating module comprises a first gas output port and a second liquid output port, and the first gas output port is connected with an absorption tower (C1); said second inlet is connected to the bottom of said active gas recovery section (C2-1); the second outlet is connected to an atmospheric vacuum flash column module (C3).
In particular, the liquid CO2The evaporator (E7) is used for evaporating gasified liquid CO2Providing a low temperature environment to cool the primary gas, CO2The liquid changes phase from high pressure to low pressure and changes from liquid state to gas state, and low temperature environment of about-55 ℃ can be provided, so that the initial gas is cooled; the (C1) is used for removing CO in the residual initial gas2And sulfide, produce and meet the purified gas of the standard requirement; the medium-low pressure flash tower (C2) is used for absorbing CO2And carrying out reduced pressure flash evaporation on the methanol-rich liquid containing sulfide to obtain CO2Gradually separated from the methanol-rich liquid.
According to the embodiment of this application, the first cooling separation module includes initial gas-clean gas heat exchanger (E1) that the input is connected with initial gas transfer pipe and with the alcohol-water knockout drum (V1) that initial gas-clean gas heat exchanger (E1) output is connected and the output with ammonia cooler (E2) that the first import is connected, the input of ammonia cooler (E2) with the top of alcohol-water knockout drum (V1) is connected, the bottom of alcohol-water knockout drum (V1) is connected with alcohol-water fractionating tower module (C6).
Specifically, an antifreeze methanol module (T) is connected to a pipeline connecting the primary gas-clean gas heat exchanger (E1) and the alcohol-water separation tank (V1), an antifreeze methanol liquid is added to the primary gas in order to prevent the liquid condensed from the primary gas from freezing in the pipeline and blocking the pipeline, and the alcohol-water separation tank (V1) is used to separate the primary gas and the antifreeze methanol liquid; the primary gas-purified gas heat exchanger (E1) performs primary cooling on the primary gas; the ammonia cooler (E2) performs secondary cooling on the initial gas; the alcohol-water fractionating tower module (C6) is used for heating, evaporating and separating methanol and water to prepare for the recycling regeneration of methanol liquid, the wastewater produced by separation enters a sewage treatment device, and the methanol steam enters the thermal regeneration tower module (C5).
According to an embodiment of the application, the second cooling separation module comprises an initial air quaternary cooling with an input connected with the first outletA liquid CO (E31) connected to the outlet of the initial gas quaternary cooler (E31)2A separation tank (V2); the liquid CO2The top of the separation tank (V2) is provided with the first gas output port, and the bottom is provided with the second liquid output port.
Specifically, the initial gas four-stage cooler (E31) performs four-stage cooling on the initial gas; the liquid CO2The separator tank (V2) is used for separating condensed liquid CO2And the remainder of the initial gas; the first gas outlet is connected to the absorption column (C1), and the second liquid outlet is connected to the upper part of the effective gas recovery section (C2-1).
According to the embodiment of the application, the absorption tower (C1) comprises a desulfurization section (C1-1), the lower part of the desulfurization section (C1-1) is connected with the first gas outlet through a pipeline, the bottom part of the desulfurization section (C1-1) is connected with the sulfur-containing methanol intermediate-pressure flash section (C2-2) through a pipeline in sequence, a filter (F1), a sulfur-containing methanol cooler (E13) and a first pressure reducing valve (K1) are arranged on the pipeline, and the position of a pipeline joint connected with the sulfur-containing methanol intermediate-pressure flash section (C2-2) is lower than that of the tower plate.
Specifically, the absorption tower (C1) comprises a desulfurization section (C1-1), a rough washing section (C1-2), a main washing section (C1-3) and a fine washing section (C1-4) from bottom to top, the lower part of the rough washing section (C1-2) is connected with the upper part of the desulfurization section (C1-1) and the upper part of a sulfur-free methanol medium-pressure flash evaporation section (C2-3) arranged in the medium-low pressure flash tower (C2) through pipelines respectively, and a second decompression valve (K2) is arranged on the pipeline connecting the lower part of the rough washing section (C1-2) and the upper part of the sulfur-free methanol medium-pressure flash evaporation section (C2-3); the lower part of the main washing section (C1-3) is connected with the upper part of the crude washing section (C1-2) through a pipeline and a methanol cooler (E4) of the main washing section of the absorption tower; the fine washing section (C1-4) lower part through the pipeline pass through absorption tower methyl alcohol ammonia cooler (E3) with main washing section (C1-3) upper portion is connected, and the top passes through the pipeline and loops through initial gas quaternary cooler (E31), initial gas-purified gas heat exchanger (E1) is connected with the purified gas collection device, just fine washing section (C1-4) upper portion is connected with methyl alcohol storage tank module (V5).
Because the produced purified gas still has lower temperature (-40 to-50 ℃), the purified gas can be used as a coolant to further reduce the energy consumption of the refrigeration of the whole system, and through the analysis of a process route, the purified gas sequentially enters an initial gas four-stage cooler (E31) and an initial gas-purified gas heat exchanger (E1) through pipelines to cool the initial gas and then enters a purified gas product collecting device, so the energy consumption of the refrigeration of the whole system is reduced.
The absorber column (C1) is used for removing CO from the residual initial gas by the methanol-poor liquid2And sulfide to produce a purified gas meeting the standard requirements, and gradually absorbing CO in the initial gas in the methanol-poor liquid2And in the sulfide process, the temperature of the poor methanol liquid is continuously increased, in order to ensure the good absorbability of the poor methanol liquid, the poor methanol liquid at the bottom of the fine washing section (C1-4) enters a main washing section (C1-3) after being cooled by an absorption tower methanol ammonia cooler (E3), and the poor methanol liquid at the bottom of the main washing section (C1-3) enters a coarse washing section (C1-2) after being cooled by a main washing section methanol cooler E4.
According to an embodiment of the application, the medium and low pressure flash column (C2) further comprises a sulfur-free methanol medium pressure flash section (C2-3), a sulfur-containing methanol low pressure flash section (C2-4), a sulfur-free methanol low pressure flash section (C2-5); the bottom of the effective gas recovery section (C2-1) is connected through the second inlet by a pipeline; the bottom of the sulfur-containing methanol medium-pressure flash section (C2-2) is connected with the upper part of the sulfur-containing methanol low-pressure flash section (C2-4) through a pipeline; the bottom of the sulfur-free methanol medium-pressure flash section (C2-3) is connected with the upper part of the sulfur-free methanol low-pressure flash section (C2-5) through a pipeline, the top of the sulfur-containing methanol medium-pressure flash section (C2-2) is connected with a pipeline, and the pipeline joint position connected with the sulfur-containing methanol medium-pressure flash section (C2-2) is lower than the tower plate.
Specifically, the bottom and the top of the sulfur-containing methanol low-pressure flash section (C2-4) are connected with an atmospheric vacuum flash tower module (C3) through pipelines; the bottom and the top of the sulfur-free methanol low-pressure flash section (C2-5) are connected with the atmospheric vacuum flash tower module (C3) through pipelines.
The atmospheric vacuum flash column module (C3) is connected to the sulfide absorber column module (C4); the sulphide absorber modules (C4) are separately associated with CO2The product gas collecting device is connected with a thermal regeneration tower module (C5); the thermal regeneration tower module (C5) is used for heating and separating out semi-lean methanol liquidSulfides in the body change the semi-lean methanol liquid into lean methanol liquid which returns to the methanol storage tank module (V5) for recycling.
The atmospheric vacuum flash tower module (C3) is used for absorbing CO2And continuing to perform reduced pressure flash evaporation on the sulfide-rich methanol liquid to further remove CO2Gradually separating from the methanol-rich liquid, and delivering the separated gas and the semi-lean methanol liquid to a sulfide absorption tower module (C4) through pipelines, wherein the gas is desulfurized and purified to produce CO in the sulfide absorption tower module (C4)2The product gas, and the semi-lean methanol liquid, enter the thermal regenerator module (C5).
The sulphide absorber module (C4) is used for purifying CO2CO after liquid gasification2The gas and the gas flashed off under reduced pressure absorb sulfide therein to produce CO meeting the standard requirements2And (5) producing gas.
The gas and the liquid flashed off under reduced pressure from the atmospheric vacuum flash tower module (C3) both have lower temperature (-40 to-55 ℃), and can further act as a coolant to reduce the energy consumption of the refrigeration of the whole system, through process route analysis, the gas flashed off under reduced pressure from the atmospheric vacuum flash tower module (C3) cools the initial gas through the initial gas-purified gas heat exchanger (E1) and then returns to enter the sulfide absorption tower module (C4), and the liquid flashed off under reduced pressure from the atmospheric vacuum flash tower module (C3) enters the sulfide absorption tower module (C4) after cooling the methanol-poor liquid in the main washing section (C1-3) through the absorption tower main washing section methanol cooler (E4); due to the CO2The product gas still has lower temperature (the temperature is-40 to-50 ℃), and can also be used as a coolant to further play a role in reducing the refrigeration energy consumption of the whole system, and the CO can be analyzed by a process route2The product gas enters into the CO after further cooling through an initial gas four-stage cooler (E31) and an initial gas-purified gas heat exchanger (E1) in sequence2And sealing the product gas collection device.
According to an embodiment of the application, the active gas circulation module comprises circulating CO2A cooler (E16), a water cooler (E14) and a gas compressor (M1); said circulating CO2Cooler (E16)) Comprises a third inlet, a third outlet, a fourth inlet and a fourth outlet; the third inlet is connected with the sulfur-containing methanol medium-pressure flash section (C2-2) through a pipeline, and the pipeline joint position connected with the sulfur-containing methanol medium-pressure flash section (C2-2) is higher than the tower plate; the gas inlet end of the gas compressor (M1) is connected with the third outlet, and the gas outlet end of the gas compressor (M1) is connected with the water cooler (E14); the other end of the water cooler (E14) is connected with the fourth inlet, and the fourth outlet is connected with an initial gas conveying pipeline which is connected with the ammonia cooler (E2) and the alcohol-water separation tank (V1).
In particular, the gas compressor (M1) is used to increase the pressure of the compressed gas, facilitating mixing with the initial gas.
According to an embodiment of the application, the trays are triple trays.
Specifically, the pressure drop of the single-layer tower plate is controlled within the range of 0.5-0.8 KPa, and the three layers of tower plates can reduce CO in effective gas2Amount of gas, CO2The gas quantity is maintained within the range of 10-15%, the pressure drop is not too high, and the energy consumption of the subsequent compressor for improving the effective gas pressure is increased.
In conclusion, the application discloses there is energy-conserving flash distillation device is washed to low temperature methyl alcohol, and the beneficial effect that produces based on above-mentioned scheme is through setting up three-layer column plate in the sulphur methyl alcohol middling pressure flash distillation section of ordinary pressure low pressure flash distillation tower to design the position of each input/output pipeline interface, obtain CO by the condensation of cooling separator2Liquid a, CO2The effective gas a obtained by the decompression flash evaporation of the liquid a in the effective gas recovery section enters the position below the three-layer tower plate of the sulfur-containing methanol medium-pressure flash evaporation section and is mixed with the gas obtained by the decompression flash evaporation of the methanol-rich liquid in the sulfur-containing methanol medium-pressure flash evaporation section to form the effective gas b, and the sulfur-containing semi-lean methanol liquid is used for washing and absorbing most of CO in the effective gas b at the three-layer tower plate of the sulfur-containing methanol medium-pressure flash evaporation section2The effective gas c is obtained, so that the volume of the effective gas c output by the sulfur-containing methanol medium-pressure flash section is reduced, the energy consumption of the effective gas c recovered by the effective gas circulation module is reduced, the energy consumption of the cooling separation device for repeatedly cooling the effective gas c is also reduced, and a condensing agent and the cooling separation device are improvedThe utilization efficiency of the method is high, and the method has high popularization and application values.
Drawings
Other features, objects and advantages of the present application will become more apparent upon reading of the following detailed description of non-limiting embodiments thereof, made with reference to the accompanying drawings.
Fig. 1 is a schematic structural diagram of a low-temperature methanol-washing energy-saving flash evaporation device in embodiment 1 of the present application.
Fig. 2 is a schematic structural diagram of a low-temperature methanol washing gas purification system using the low-temperature methanol washing energy-saving flash evaporation device in embodiment 1 of the present application.
Wherein,
c1: an absorption tower; c1-1: a desulfurization section; c1-2: a rough washing section; c1-3: a main washing section; c1-4: a fine washing section; c2: a medium and low pressure flash column; c2-1: an effective gas recovery section; c2-2: a sulfur-containing methanol medium-pressure flash evaporation section; c2-3: a sulfur-free methanol medium-pressure flash evaporation section; c2-4: a sulfur-containing methanol low-pressure flash evaporation section; c2-5: a sulfur-free methanol low-pressure flash evaporation section; c3: an atmospheric vacuum flash tower module; c3-1: a sulfur-containing methanol vacuum flash evaporation section; c3-2: a sulfur-containing methanol normal-pressure flash evaporation section; c3-3: a sulfur-free methanol vacuum flash section; c3-4: a sulfur-free methanol normal-pressure flash evaporation section; c4: a sulfide absorber module; c5: a thermal regeneration tower module; c6: an alcohol-water fractionation column module; c41: a fifth outlet; c42: a fifth inlet.
E1: a primary gas-purified gas heat exchanger; e2: an ammonia cooler; e3: a methanol ammonia cooler of the absorption tower; e31: an initial gas quaternary cooler; e4: a methanol cooler at the main washing section of the absorption tower; e5: a methanol-lean precooler; e6: a primary preheater; e7: liquid CO2An evaporator; e13: a sulfur-containing methanol cooler; e14: a water cooler; e16: recycling CO2A cooler.
V1: an alcohol-water separation tank; v2: liquid CO2A separation tank; v5: a methanol storage tank module.
P1: make-up/freeze methanol feed pumps; p2: a sulfide absorption tower feed pump; p3: a medium-pressure flash tower feed pump; p4: a sulfur-containing methanol circulating pump; p5: and a sulfide absorption tower extraction pump.
J1: a sulfur-free CO2 eductor; j2: a sulfur-containing CO2 eductor; m1: a gas compressor; f1: a filter; k1: a first pressure reducing valve; k2: a second pressure reducing valve; t: an anti-freezing methanol module.
Detailed Description
The present application will be described in further detail with reference to the following drawings and examples. It is to be understood that the specific embodiments described herein are merely illustrative of the relevant invention and not restrictive of the invention. It should be noted that, for convenience of description, only the portions related to the present invention are shown in the drawings.
The present application will now be described in detail with reference to the drawings, in conjunction with the following examples.
Example 1
The low-temperature methanol washing energy-saving flash evaporation device shown in the figure 1 comprises an absorption tower C1 and a medium-low pressure flash evaporation tower C2, wherein the medium-low pressure flash evaporation tower C2 comprises an effective gas recovery section C2-1, a sulfur-containing methanol medium-pressure flash evaporation section C2-2, a sulfur-free methanol medium-pressure flash evaporation section C2-3, a sulfur-containing methanol low-pressure flash evaporation section C2-4 and a sulfur-free methanol low-pressure flash evaporation section C2-5;
a three-layer tower plate is arranged in the sulfur-containing methanol medium-pressure flash evaporation section C2-2;
the upper part of the effective gas recovery section (C2-1) is provided with a pipeline connected with the sulfur-containing methanol medium-pressure flash section (C2-2), the position of a pipeline joint connected with the sulfur-containing methanol medium-pressure flash section (C2-2) is lower than the tower plate, and the effective gas recovery section is also provided with a pipeline used for condensing and separating CO in the initial gas2Obtaining CO2A pipeline connected with a second liquid output port of the cooling and separating device for the liquid a and the gas a; the sulfur-containing methanol medium-pressure flash evaporation section (C2-2) is provided with a methanol liquid input pipeline, the pipeline interface position is higher than the tower plate, a pipeline connected with an effective gas circulation module is also arranged, the pipeline interface position is higher than the tower plate, and the other end of the effective gas circulation module is connected with the cooling separation device.
Further, the cooling separation device comprises a first cooling separation module and liquid CO2An evaporator E7 and a second cooling and separating module;
the liquid CO2The evaporator E7 includes a first inlet, a first outlet, a second inlet, a second outlet;
the output end of the first cooling and separating module is connected with the first inlet, and the input end of the first cooling and separating module is connected with an initial gas conveying pipeline; the input end of the second cooling and separating module is connected with the first outlet, the output end of the second cooling and separating module comprises a first gas output port and a second liquid output port, and the first gas output port is connected with the absorption tower C1; the second inlet is connected with the bottom of the effective gas recovery section C2-1; the second outlet is connected to a sulfide absorber module C3.
Further, the first cooling and separating module comprises an initial gas-purified gas heat exchanger E1 with an input end connected with an initial gas conveying pipeline, an alcohol-water separating tank V1 with an output end connected with an output end of the initial gas-purified gas heat exchanger E1, an ammonia cooler E2 with an output end connected with the first inlet, an input end of the ammonia cooler E2 is connected with the top of the alcohol-water separating tank V1, the bottom of the alcohol-water separating tank V1 is connected with an alcohol-water fractionating tower module C6, and an antifreezing methanol module T is connected on a pipeline connecting the initial gas-purified gas heat exchanger E1 with the alcohol-water separating tank V1.
Further, the second cooling and separating module comprises an initial gas four-stage cooler E31 with an input end connected with the first outlet and liquid CO connected with the other end of the initial gas four-stage cooler E312Separator V2; the liquid CO2The first gas outlet at the top of the knockout drum V2 is connected with the absorption column C1, and the second liquid outlet at the bottom is connected with the upper part of the effective gas recovery section C2-1.
Further, the absorption tower C1 comprises a desulfurization section C1-1, a rough washing section C1-2, a main washing section C1-3 and a fine washing section C1-4 from bottom to top, the lower part of the desulfurization section C1-1 is connected with the first gas outlet through a pipeline, the bottom of the desulfurization section C1-1 is connected with the sulfur-containing methanol medium-pressure flash evaporation section C2-2 through a filter F1, a sulfur-containing methanol cooler E13 and a first pressure reducing valve K1 in sequence, and the position of a pipeline interface connected with the sulfur-containing methanol medium-pressure flash evaporation section C2-2 is lower than the tower plate; the lower part of the rough washing section C1-2 is respectively connected with the upper part of the desulphurization section C1-1 and the upper part of a sulfur-free methanol medium-pressure flash evaporation section C2-3 arranged in the medium-low pressure flash tower C2 through pipelines, and a pressure reduction valve II K2 is arranged on a pipeline connecting the lower part of the rough washing section C1-2 and the upper part of the sulfur-free methanol medium-pressure flash evaporation section C2-3; the lower part of the main washing section C1-3 is connected with the upper part of the crude washing section C1-2 through a pipeline and a main washing section methanol cooler E4 of an absorption tower; the lower part of the fine washing section C1-4 passes through an absorption tower methanol ammonia cooler E3 through a pipeline and is connected with the upper part of the main washing section C1-3, the top passes through the initial gas four-stage cooler E31 through a pipeline, the initial gas-purified gas heat exchanger E1 is connected with a purified gas collecting device, and the upper part of the fine washing section C1-4 is connected with a methanol storage tank module V5.
Further, the medium-low pressure flash tower C2 further comprises a sulfur-free methanol medium-pressure flash section C2-3, a sulfur-containing methanol low-pressure flash section C2-4 and a sulfur-free methanol low-pressure flash section C2-5; the bottom of the effective gas recovery section C2-1 is connected through a second inlet by a pipeline; the bottom of the sulfur-containing methanol medium-pressure flash section C2-2 is connected with the upper part of the sulfur-containing methanol low-pressure flash section C2-4 through a pipeline, and the upper part is connected with circulating CO through a pipeline2A third inlet on cooler E16, the recycle CO2A third outlet of the cooler E16 is connected with the gas inlet end of a gas compressor M1 through a pipeline, the gas outlet end of the gas compressor M1 is connected with a water cooler E14, and the other end of the water cooler E14 is connected with the circulating CO2A fourth inlet connection on cooler E16, the recycle CO2A fourth outlet on the cooler E16 is connected with an initial gas conveying pipeline which is connected with the ammonia cooler E2 and the alcohol-water separation tank V1; the bottom of the sulfur-free methanol medium-pressure flash section C2-3 is connected with the upper part of the sulfur-free methanol low-pressure flash section C2-5 through a pipeline, the top of the sulfur-containing methanol medium-pressure flash section C2-2 is connected with a pipeline, and the position of a pipeline joint connected with the sulfur-containing methanol medium-pressure flash section C2-2 is lower than the tower plate; the bottom and the top of the sulfur-containing methanol low-pressure flash section C2-4 are connected with an atmospheric vacuum flash tower module C3 through pipelines; the bottom and the top of the sulfur-free methanol low-pressure flash section C2-5 are communicated with an atmospheric vacuum flash tower module C3 through pipelines.
Further, the gas output end of the atmospheric vacuum flash tower module C3 is connected with the sulfide absorption tower module C4 after passing through the initial gas-purified gas heat exchanger E1 through a pipeline; the liquid output end of the atmospheric vacuum flash tower module C3 passes through the absorption tower main washing section methanol cooler E4 through a pipeline and then is connected with the sulfide absorption tower module C4;
further, the gas output end of the sulfide absorption tower module C4 passes through the initial gas four-stage cooler E31, the initial gas-purified gas heat exchanger E1 and the CO in sequence through pipelines2The product gas collection device is connected, and the liquid output end of the sulfide absorption tower module C4 is connected with the thermal regeneration tower module C5.
Example 2
As shown in fig. 2, a schematic structural diagram of a low-temperature methanol washing gas purification system using the low-temperature methanol washing energy-saving flash apparatus of embodiment 1 is shown, where the low-temperature methanol washing gas purification system of fig. 2 is used to purify an initial gas generated by coal-to-methanol process, the initial gas pressure is about 3.56MPa, and the composition is as follows: 43% H2、19.4％CO、36.2％CO2、0.69％H2S and other component gases, the main treatment process is as follows:
the initial gas (the temperature is about 30 ℃) is cooled to about 0 ℃ through an initial gas-purified gas heat exchanger E1, the initial gas is mixed with the sulfur-free semi-lean methanol liquid h for freeze protection from a sulfur-free methanol vacuum flash evaporation section C3-3 and then enters an alcohol-water separation tank V1, the sulfur-free semi-lean methanol liquid i (the temperature is about 0 ℃ and the pressure is about 3.6MPa) and the gas i (the temperature is 0 ℃ and the pressure is 3.6MPa) are separated through an alcohol-water separation tank V1,
the gas i is output from the top of an alcohol-water separation tank V1, mixed with effective gas C from a sulfur-containing methanol medium-pressure flash evaporation section C2-2, enters an ammonia cooler E2, cooled to minus 10 to minus 20 ℃ by an ammonia cooler E2, and enters liquid CO from a first inlet2The evaporator E7 was further cooled to a temperature of-47 to-53 ℃ at which time part of the CO in the gas i was present2Condensed into liquid phase, output from the first outlet, enter an initial gas four-stage cooler E31 for further cooling and reducing the temperature to-55 to-57 ℃, and further condense CO in the gas i2Then into liquid CO2Separating in a separating tank V2 to obtain CO2Liquid a (temperature is about-53 ℃ and pressure is about 3.55 MPa) and gas a (temperature is about-53 ℃ and pressure is about 3.55 MPa),
the gas a is derived from liquid CO2A first gas output port at the top of the separation tank V2 is output, enters a desulfurization section C1-1 of an absorption tower C1 for desulfurization, and then sequentially enters a rough washing section C1-2 and a main washing section C1-3 to remove most of residual CO in gas a2Finally, the poor methanol liquid in the fine washing section C1-4 is further treated to produce purified gas meeting the requirements, the temperature of the purified gas is-45 to-55 ℃, the pressure is about 3.6MPa, and CO is used for purifying the poor methanol liquid in the fine washing section C1-42The content is less than 20ppm, and the sulfide content is less than 1 ppm. Because the purified gas still has lower temperature and can be used as a refrigerant to provide cold for the system, the purified gas sequentially enters the initial gas four-stage cooler E31 through a pipeline to carry out four-stage cooling on the gas i, enters the initial gas-purified gas heat exchanger E1 to carry out primary cooling on the initial gas and then enters the purified gas product collection device. The poor methanol liquid for purifying the gas a in the process is from a methanol storage tank module V5, the poor methanol liquid at about-60 ℃ enters from an upper fine washing section C1-4 of an absorption tower C1, and then sequentially enters a main washing section C1-3, a coarse washing section C1-2 and a desulfurization section C1-1 to absorb CO step by step2Sulphides, gradual absorption of CO in gas a in methanol-lean liquid2In the process of sulfide, the temperature of poor methanol liquid is continuously increased, in order to ensure good absorptivity of the poor methanol liquid, the poor methanol liquid at the bottom of a fine washing section C1-4, which is at about-30 ℃, is cooled to about-55 ℃ by an absorption tower methanol ammonia cooler E3 and then enters a main washing section C1-3, and the poor methanol liquid at the bottom of the main washing section C1-3, which is at about-35 ℃, is cooled to about-45 ℃ by a main washing section methanol cooler E4 and then enters a coarse washing section C1-2.
The sulfur-free semi-lean methanol liquid i is output from the bottom of the alcohol-water separation tank V1 and enters an alcohol-water fractionating tower module C6 through a pipeline, in the alcohol-water fractionating tower module C6, methanol in the heated sulfur-free semi-lean methanol liquid i is evaporated and gasified to enter a thermal regeneration tower module C5 for regeneration and recycling, and the residual wastewater flows out of the alcohol-water fractionating tower module C6 and enters a sewage treatment system.
From liquid CO2CO output by a second liquid output port at the bottom of the separation tank V22The liquid a enters an effective gas recovery section C2-1 of a medium-low pressure flash tower C2 through a pipeline, and effective gas a and CO are obtained through reduced pressure flash evaporation2Liquid b (temperature-about 53 ℃ C., temperature about 1.0 MPa)The temperature of the effective gas a is about-35 ℃, the pressure is about 1.0MPa, and the effective gas a comprises 5-8% of H2And CO, which enters the three-layer tray below the sulfur-containing methanol medium-pressure flash section C2-2 through a pipeline.
Absorption of CO in absorption column C12The methanol-poor liquid with sulfide is changed into methanol-rich liquid a, the methanol-rich liquid a comprises sulfur-containing methanol-rich liquid C and sulfur-free methanol-rich liquid d, and the sulfur-containing methanol-rich liquid C (with the temperature of about-25 ℃, the pressure of about 3.6MPa and CO content and output from the bottom of a desulfurization section C1-1 of an absorption tower C125-8%) of the methanol, sequentially passing through a filter F1, cooling to-28 ℃ through a sulfur-containing methanol cooler E13, reducing the pressure to 1.0MPa through a pressure reduction valve K1, entering a sulfur-containing methanol medium-pressure flash section C2-2 below three layers of tower plates, and performing pressure reduction flash evaporation to obtain a sulfur-containing methanol-rich liquid E (the temperature is about-45 ℃ and the pressure is about 0.9 MPa) and a gas E (the temperature is about-45 ℃ and the pressure is about 0.9 MPa), wherein the gas E comprises CO2And sulfides, mixed with the utility gas a from utility gas recovery section C2-1.
Sulfur-free methanol-rich liquid d (temperature about-25 deg.C, pressure about 3.6MPa, CO) output from the crude washing section C1-2 of the absorption tower C1240 percent of the sulfur content of the methanol gas enters a desulfurization section C1-1 to continuously absorb sulfide in the gas a, the other part of the sulfur content of the methanol gas can be decompressed to 1.0MPa through a decompression valve II K2 according to requirements, then enters a sulfur-free methanol medium-pressure flash evaporation section C2-3, and is subjected to decompression flash evaporation to obtain sulfur-free methanol-rich liquid f (the temperature is about-45 ℃ and the pressure is about 0.9 MPa) and gas f (the temperature is about-45 ℃ and the pressure is 0.9MPa and CO is2The content of 10 percent), the gas f enters a middle-pressure flash evaporation section C2-2 of the sulfur-containing methanol below three layers of tower plates to be mixed with the effective gas a and the gas e to obtain the effective gas b (the temperature is minus 40 to minus 45 ℃, the pressure is about 0.9MPa, and the effective gas b contains about 55 percent of CO2) Washing and absorbing most of CO in the sulfur-containing semi-lean methanol liquid g2Then obtaining effective gas C (the temperature is between 40 ℃ below zero and 50 ℃ below zero and the pressure is about 0.9 MPa), discharging the effective gas C from the top of a medium-pressure flash evaporation section C2-2 of the sulfur-containing methanol, and introducing the effective gas C into circulating CO2The cooler E16 exchanges heat and heats to about-25 ℃, then enters the gas compressor M1, is pressurized to 3.6MPa by the compressor M1, and then enters the water cooler E14 to cool to about-30 DEG CThen re-enter the cycle CO2Cooler E16, circulating CO2The cooler E16 cools to about-35 deg.C, and the mixture is mixed with gas i via pipeline and further cooled in the ammonia cooler E2. In order to reduce the volume of the compressed effective gas C, at the three-layer tray of the sulfur-containing methanol medium-pressure flash section C2-2, sulfur-containing semi-lean methanol liquid g (with the temperature of-45 ℃, the pressure of 0.15MPa and CO) from the bottom of the sulfur-containing methanol vacuum flash section C3-1 in the atmospheric vacuum flash tower module C3 is contained210%) will absorb about 70-75% of the CO in the effective gas b2Gas, thereby reducing CO re-entering gas i2The volume of the effective gas c is reduced, so that the CO is increased2The recovery rate also reduces the power consumption of the compressor M1.
And sulfur-free methanol-rich liquid f (temperature about 40 ℃ below zero, pressure about 1.0MPa and CO) output from the bottom of the sulfur-free methanol medium-pressure flash evaporation section C2-32The content of 10 percent) enters a low-pressure flash evaporation section C2-5 of the sulfur-free methanol, and sulfur-free CO is further flashed out by decompression2Gas h1(temperature is about-45 ℃, pressure is about 0.6MPa, CO2Content 35%) and the gas b enter the atmospheric vacuum flash tower module C3 after being mixed2Injector J1 inlet end as sulfur free CO2Motive gas of an ejector J1, and sulfur-free methanol-rich liquid h output from the bottom of a sulfur-free methanol low-pressure flash section C2-51(temperature is about-45 ℃, pressure is about 0.6MPa, CO2The content is 5 percent) enters a sulfur-free methanol atmospheric flash section C3-4 in the atmospheric vacuum flash tower module C3, and sulfur-free CO is further flashed in a reduced pressure manner2Gas h2(temperature is about 50 ℃ below zero and pressure is about 0.1 MPa), and is communicated with sulfur-free CO through a pipeline2The gas outlet end of the ejector J1 is merged, and sulfur-free methanol-rich liquid h is output from the bottom of the sulfur-free methanol normal-pressure flash evaporation section C3-42(temperature-50 ℃ or so, pressure 0.1MPa or so, CO)21-3%) of the sulfur-free methanol enters a sulfur-free methanol vacuum flash evaporation section C3-3 in the normal pressure vacuum flash evaporation tower module C3, and sulfur-free CO is further flashed out in a reduced pressure manner2Gas h3(temperature is about-65 ℃ and pressure is about 0.02 MPa) and is coated with sulfur-free CO2Ejector J1, in sulfur-free CO2Outlet and outlet ports of injector J1Sulfur-free CO flashed from sulfur methanol atmospheric flash section C3-42Gas h2Converging to obtain gas h (temperature of about-65 ℃ and pressure of about 0.02 MPa), and obtaining sulfur-free semi-lean methanol liquid h (temperature of about-65 ℃ and pressure of about 0.02 MPa) in the sulfur-free methanol vacuum flash evaporation section C3-3 at the moment2The content of the sulfur-free semi-lean methanol liquid h output from the bottom of the sulfur-free methanol vacuum flash evaporation section C3-3 is divided into three parts, the first part is mixed with initial gas through a supplement/antifreezing methanol feed pump P1 in the normal pressure vacuum flash tower module C3 and then enters an alcohol-water separation tank V1 for antifreezing, and the second part enters a main washing section C1-3 through a supplement/antifreezing methanol feed pump P1 and is used for continuously absorbing CO in the gas a2The third part of the gas enters the upper part of a sulfide absorption tower module C4 through a sulfide absorption tower feed pump P2 in the atmospheric vacuum flash tower module C3 and is used for removing sulfide in the gas d.
Sulfur-containing methanol-rich liquid e (temperature-40 deg.C, pressure 1.0MPa, CO) output from the bottom of sulfur-containing methanol medium-pressure flash section C2-225 percent of sulfide and less than 0.5 percent of sulfide enter a sulfur-containing methanol low-pressure flash evaporation section C2-4 through a pipeline, and partial sulfur-containing CO is flashed off through decompression2Gas g1(temperature-45 ℃ or so, pressure 0.6MPa or so, CO)2Content 10%) of sulfur-containing CO mixed with the gas b and entering the atmospheric vacuum flash tower module C32Injector J2 as sulfur-containing CO2Motive gas of an ejector J2, and sulfur-containing methanol-rich liquid g output from the bottom of a sulfur-containing methanol low-pressure flash section C2-41(temperature-45 ℃, pressure 0.6MPa, CO)2The content of 3 percent and the sulfide is less than 0.5 percent) enters a sulfur-containing methanol normal-pressure flash evaporation section C3-2 in the normal-pressure vacuum flash evaporation tower module C3, and partial sulfur-containing CO is further flashed in a reduced pressure manner2Gas g2(temperature-50 ℃ or so, pressure 0.1MPa or so, CO)28%) in the gas mixture is mixed with sulfur-containing CO through a pipeline2The gas outlet ends of the ejectors J2 are merged, and sulfur-containing methanol-rich liquid g is output from the bottom of a sulfur-containing methanol atmospheric pressure flash section C3-22(temperature-50 ℃ or so, pressure 0.1MPa or so, CO)2The content of 3 percent and the sulfide is less than 0.5 percent) enters a sulfur-containing methanol vacuum flash section C3-1 in the atmospheric vacuum flash tower module C3 and then entersOne-step reduced pressure flash distillation of sulfur-containing CO2Gas g3(temperature is about-65 ℃ and pressure is about 0.02 MPa) and is coated with sulfur-containing CO2Ejector J2, in sulfur-containing CO2The outlet end of the injector J2 is connected with sulfur-containing CO2Gas g1CO containing sulfur2Gas g2Then the mixture is converged to obtain gas g (the temperature is about-65 ℃ and the pressure is about 0.02 MPa). At the moment, sulfur-containing methanol vacuum flash evaporation section C3-1 obtains sulfur-containing semi-lean methanol liquid g (the temperature is about 65 ℃ below zero, the pressure is about 0.02MPa, CO is2The content of sulfur-containing semi-lean methanol liquid g is 2 percent, the sulfide content is less than 0.5 percent, the sulfur-containing semi-lean methanol liquid g output from the bottom of the sulfur-containing methanol vacuum flash section C3-1 is divided into two parts, the first part enters the sulfur-containing methanol intermediate-pressure flash section C2-2 three layers of tower plates through an intermediate-pressure flash tower feed pump P3 in the atmospheric vacuum flash tower module C3 and is used for continuously absorbing CO in the effective gas b2And the second part of the liquid lean methanol enters the middle part of a sulfide absorption tower module C4 for sulfide removal after passing through a sulfur-containing methanol circulating pump P4 in the atmospheric vacuum flash tower module C3 and cooling the lean methanol liquid in a main washing section C1-3 of the absorption tower through a main washing section methanol cooler E4.
CO output from the bottom of the effective gas recovery section C2-12Liquid b enters the liquid CO from the second inlet2Evaporator E7 through the liquid CO2Evaporator E7 Depressation, CO2The liquid b is changed from high pressure to low pressure to be in a phase change state from a liquid state to a gas state to obtain gas b (the temperature is about-55 ℃, and the pressure is about 0.6 MPa), the gas b can provide a low-temperature environment about-55 ℃ to realize the cooling of the gas i, and meanwhile, the gas b is output from the second outlet and respectively enters the sulfur-free CO through the pipelines2Eductor J1 and sulfur-containing CO2Inlet end of injector J2 as sulfur-free CO2Injector J1 and Sulfur-containing CO2Motive power of injector J2 to reduce sulfur free CO2Injector J1 and Sulfur-containing CO2Energy consumption of injector J2.
In the absence of sulfur CO respectively2Injector J1 and Sulfur-containing CO2Sulfur-free CO merging at the outlet end of injector J22Gas h and sulfur-containing CO2The gas g is converged through a pipeline to form a gas c, the gas c is mixed with the gas b to obtain a gas d, and the gas d is (temperature-About 55 ℃ and about 0.1MPa in pressure) is heated by an initial gas-purified gas heat exchanger E1 (at the moment, the temperature of the gas d is about 35 ℃ below zero) and enters a sulfide absorption tower module C4 to carry out sulfide removal so as to purify the gas d, the purified gas d (at the moment, the temperature is about 55 ℃ below zero and the pressure is about 0.6 MPa) is output from the top of a sulfide absorption tower C4, and the gas d reaches CO at the moment2Standard for product gas recovery (CO)2Content 99.99%), but still at a lower temperature, can further act as a coolant to reduce the cooling demand energy consumption of the entire system, and so is in turn H2S cooler E12 cools H2Gas k of S1Carrying out four-stage cooling on the gas i by an initial gas four-stage cooler E31, carrying out first-stage cooling on the initial gas by an initial gas-purified gas heat exchanger E1, and then feeding the initial gas into CO2The product gas collection device is sealed (the temperature is about-20 ℃, the pressure is about 0.6MPa, and CO is generated2Content 99.99%).
The sulfur-containing semi-lean methanol liquid g and the sulfur-free semi-lean methanol liquid h are converged at the lower part of the sulfide absorption tower module C4 to obtain the semi-lean methanol liquid b (the temperature is about-40 to-50 ℃, the pressure is 0.1 to 0.3MPa, and CO is used as a catalyst for the absorption of sulfur compounds in the semi-lean methanol liquid b)2The content of the semi-lean methanol liquid b is 3% and the sulfide content is less than 0.5%), at the moment, the semi-lean methanol liquid b still has a lower temperature, the function of a refrigerant can be fully utilized, the energy consumption of system refrigeration is reduced, in order to fully utilize the part of energy and further reduce the energy consumption required by the refrigeration of the whole system, the semi-lean methanol liquid b in the sulfide absorption tower module C4 is extracted from a fifth outlet C41, the sulfur-containing methanol cooler E13 cools the sulfur-containing methanol-rich liquid C output from the bottom of the desulfurization section C1-1, and then the sulfur-containing methanol-rich liquid C returns to the lower part of the sulfide absorption tower module C4 from a fifth inlet C42.
Semi-lean methanol liquid b (with the temperature of about-10 ℃, the pressure of 0.1-0.3 MPa and CO) output from the bottom of the sulfide absorption tower module C42The content of 3 percent and the sulfide is less than 0.5 percent) enters a thermal regeneration tower module C5 through a sulfide absorption tower extraction pump P5 to remove the sulfide so as to purify the semi-lean methanol liquid b into lean methanol liquid which enters a methanol storage tank module V5 for recycling, and simultaneously the generated sulfide gas enters a sulfide recovery device.
It can be seen from the above examples that the present application provides an energy-saving flash evaporation apparatus for low-temperature methanol washing, wherein three layers of tower plates are arranged in the sulfur-containing methanol intermediate-pressure flash evaporation section C2-1 of the normal-pressure low-pressure flash evaporation tower C2, and the position of each input/output pipeline interface is designed, so that most of CO in the effective gas b in the sulfur-containing methanol intermediate-pressure flash evaporation section C2-12The sulfur-containing semi-lean methanol liquid is used for washing and absorbing at the three-layer tower plate, so that the volume of effective gas C output by a sulfur-containing methanol medium-pressure flash evaporation section C2-1 is reduced, the energy consumption of the effective gas C compressed by a compressor M1 is further reduced, the amount of the effective gas C repeatedly entering a cooling separation device is also reduced, the energy consumption of the effective gas C repeatedly cooled by the cooling separation device is reduced, the utilization efficiency of a condensing agent and the cooling separation device is improved, and the method has high popularization and application values.
It can also be seen that the heat is passed through the primary gas-purified gas heat exchanger (E1), the ammonia chiller (E2), the liquid CO2Evaporator (E7), initial gas four-stage cooler (E31) four-stage cooling, about 40% CO in the initial gas2Condensed into CO2Liquid a, and residual gas a, CO obtained after separation2The liquid a is subjected to reduced pressure flash evaporation to obtain effective gas a and CO2Liquid b and make full use of CO2The liquid b has the characteristics of high pressure and low temperature, is changed into gas b after evaporation and gasification to be used as the power of the whole system ejector, reduces the energy consumption of the whole system ejector, and adopts the poor methanol liquid to absorb the other part of CO in the gas a2Recovering the gas C through gradual reduced pressure flash evaporation, and finally mixing the two parts of gas b and the gas C and then entering a sulfide absorption tower C4 for desulfurization treatment to obtain CO2Product gas realizes CO in the initial gas2Almost completely trapping and recovering, sealing under pressure, convenient use, and about 40% of CO in the initial gas2Without absorption and removal of methanol-lean liquid, thereby removing CO2The consumption of the poor methanol liquid is reduced by 30-45%, the energy consumption for recovering the poor methanol liquid is also reduced by 30-45%, and the consumption of the circulating poor methanol liquid is greatly reduced, so that the tower diameter of each treatment tower can be reduced, the equipment is miniaturized, and the method has high popularization and application values.
It should be understood that the above-described embodiments of the present invention are merely examples for clearly illustrating the invention and are not intended to limit the embodiments of the present invention, and that various other modifications and changes can be made on the basis of the above description by those skilled in the art.
Claims (8)
1. A low-temperature methanol washing energy-saving flash evaporation device comprises a device for washing the liquid containing CO2And a medium-low pressure flash column (C2) for the reduced pressure flash distillation of the methanol-rich liquid with sulphide, characterized in that the medium-low pressure flash column (C2) comprises a reactor for reacting CO with a liquid rich in methanol2An effective gas recovery section (C2-1) for obtaining an effective gas a by flashing the liquid a under reduced pressure and a method for absorbing CO2A sulfur-containing methanol medium-pressure flash section (C2-2) outputting effective gas C; a tower plate is arranged in the sulfur-containing methanol medium-pressure flash section (C2-2);
the upper part of the effective gas recovery section (C2-1) is provided with a pipeline connected with the sulfur-containing methanol medium-pressure flash section (C2-2), the position of a pipeline joint connected with the sulfur-containing methanol medium-pressure flash section (C2-2) is lower than the tower plate, and the effective gas recovery section is also provided with a pipeline used for condensing and separating CO in the initial gas2Obtaining CO2A pipeline connected with a second liquid output port of the cooling and separating device for the liquid a and the gas a; the sulfur-containing methanol medium-pressure flash evaporation section (C2-2) is provided with a methanol liquid input pipeline, the pipeline interface position is higher than the tower plate, a pipeline connected with an effective gas circulation module is also arranged, the pipeline interface position is higher than the tower plate, and the other end of the effective gas circulation module is connected with the cooling separation device.
2. The low-temperature methanol washing energy-saving flash evaporation device according to claim 1, wherein the cooling separation device comprises a first cooling separation module, liquid CO2An evaporator (E7) and a second cooling and separating module; the liquid CO2The evaporator (E7) comprises a first inlet, a first outlet, a second inlet and a second outletA mouth;
the output end of the first cooling and separating module is connected with the first inlet, and the input end of the first cooling and separating module is connected with an initial gas conveying pipeline; the input end of the second cooling and separating module is connected with the first outlet, the output end of the second cooling and separating module comprises a first gas output port and a second liquid output port, and the first gas output port is connected with an absorption tower (C1); said second inlet is connected to the bottom of said active gas recovery section (C2-1); the second outlet is connected to an atmospheric vacuum flash column module (C3).
3. The low-temperature methanol washing energy-saving flash device according to claim 2, wherein the first cooling separation module comprises an initial gas-purified gas heat exchanger (E1) with an input end connected with an initial gas conveying pipeline, an alcohol-water separation tank (V1) connected with an output end of the initial gas-purified gas heat exchanger (E1), and an ammonia cooler (E2) with an output end connected with the first inlet, wherein the input end of the ammonia cooler (E2) is connected with the top of the alcohol-water separation tank (V1), and the bottom of the alcohol-water separation tank (V1) is connected with the alcohol-water fractionating tower module (C6).
4. The low-temperature methanol-washing energy-saving flash device according to claim 3, wherein the second cooling and separating module comprises an initial gas four-stage cooler (E31) with an input end connected with the first outlet and liquid CO connected with an output end of the initial gas four-stage cooler (E31)2A separation tank (V2); said liquid CO2The top of the separation tank (V2) is provided with the first gas output port, and the bottom is provided with the second liquid output port.
5. The low-temperature methanol washing energy-saving flash device as claimed in claim 4, wherein the absorption tower (C1) comprises a desulfurization section (C1-1), the lower part of the desulfurization section (C1-1) is connected with the first gas outlet through a pipeline, the bottom of the desulfurization section (C1-1) is connected with the sulfur-containing methanol medium-pressure flash section (C2-2) through a filter (F1), a sulfur-containing methanol cooler (E13) and a first pressure reducing valve (K1) in sequence through pipelines, and the position of a pipeline joint connected with the sulfur-containing methanol medium-pressure flash section (C2-2) is lower than the tower plate.
6. The low-temperature methanol washing energy-saving flash evaporation device as claimed in claim 4, wherein the medium-low pressure flash evaporation tower (C2) further comprises a sulfur-free methanol medium-pressure flash evaporation section (C2-3), a sulfur-containing methanol low-pressure flash evaporation section (C2-4) and a sulfur-free methanol low-pressure flash evaporation section (C2-5); the bottom of the effective gas recovery section (C2-1) is connected through the second inlet by a pipeline; the bottom of the sulfur-containing methanol medium-pressure flash section (C2-2) is connected with the upper part of the sulfur-containing methanol low-pressure flash section (C2-4) through a pipeline; the bottom of the sulfur-free methanol medium-pressure flash section (C2-3) is connected with the upper part of the sulfur-free methanol low-pressure flash section (C2-5) through a pipeline, the top of the sulfur-containing methanol medium-pressure flash section (C2-2) is connected with a pipeline, and the pipeline joint position connected with the sulfur-containing methanol medium-pressure flash section (C2-2) is lower than the tower plate.
7. The low-temperature methanol washing energy-saving flash evaporation device according to claim 6, wherein the effective gas circulation module comprises circulating CO2A cooler (E16), a water cooler (E14) and a gas compressor (M1); said circulating CO2The cooler (E16) comprises a third inlet, a third outlet, a fourth inlet and a fourth outlet; the third inlet is connected with the sulfur-containing methanol medium-pressure flash section (C2-2) through a pipeline, and the pipeline joint position connected with the sulfur-containing methanol medium-pressure flash section (C2-2) is higher than the tower plate; the gas inlet end of the gas compressor (M1) is connected with the third outlet, and the gas outlet end of the gas compressor (M1) is connected with the water cooler (E14); the other end of the water cooler (E14) is connected with the fourth inlet, and the fourth outlet is connected with an initial gas conveying pipeline which is connected with the ammonia cooler (E2) and the alcohol-water separation tank (V1).
8. The low-temperature methanol washing energy-saving flash evaporation device as claimed in any one of claims 1 to 7, wherein the tower plate is a three-layer tower plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220168202.7U CN216934749U (en) | 2022-01-21 | 2022-01-21 | Energy-conserving flash distillation plant is washed to low temperature methyl alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220168202.7U CN216934749U (en) | 2022-01-21 | 2022-01-21 | Energy-conserving flash distillation plant is washed to low temperature methyl alcohol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216934749U true CN216934749U (en) | 2022-07-12 |
Family
ID=82317164
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202220168202.7U Active CN216934749U (en) | 2022-01-21 | 2022-01-21 | Energy-conserving flash distillation plant is washed to low temperature methyl alcohol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216934749U (en) |
-
2022
- 2022-01-21 CN CN202220168202.7U patent/CN216934749U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101456556B (en) | A device and method for industrial separation and purification of CO2 in mixed gas by hydrate method | |
| CN102115684B (en) | Method for producing liquefied natural gas from coke oven gas | |
| CN106281476B (en) | A kind of method of sour gas in low temperature washing device for methanol and a kind of removing synthesis gas | |
| CN201729816U (en) | Liquid nitrogen washing device for purifying synthesis gas | |
| CN111303945A (en) | Low-temperature methanol washing process method and device with low energy consumption and high carbon capture rate | |
| CN109294645A (en) | It is a kind of to utilize coke-stove gas synthesis of methanol with joint production LNG, richness H2Device and method | |
| CN103497801B (en) | A kind of technique utilizing carbon black tail gas to prepare synthetic natural gas | |
| CN103695043B (en) | Method for drying, purifying and cooling conversion rough synthesized gas and SNG product gas through low-temperature methanol washing and device thereof | |
| CN104987279B (en) | Methanol-making system and method through coal gasification integrating waste heat cooling and carbon trapping | |
| CN212560126U (en) | A low-temperature methanol washing process device with low energy consumption and high carbon capture rate | |
| CN216934749U (en) | Energy-conserving flash distillation plant is washed to low temperature methyl alcohol | |
| CN212316051U (en) | Poly-generation device for producing natural gas by using underground gasified gas | |
| CN113061475A (en) | Liquefaction process method and device for separating carbon dioxide from critical biogas by adjusting concentration of carbon dioxide | |
| CN216987001U (en) | Low-temperature methanol-washed CO2Cooling and separating device | |
| CN209052640U (en) | It is a kind of to utilize coke-stove gas synthesis of methanol with joint production LNG, richness H2Device | |
| CN217715638U (en) | Shale gas edulcoration rectification separation and liquefaction equipment | |
| CN114470847B (en) | A system for separating and purifying CO2 | |
| CN114470846B (en) | A gas purification method | |
| CN112979516B (en) | Energy-saving methyl mercaptan synthesis device | |
| CN111004082A (en) | System and method for removing carbon dioxide from C2 fraction | |
| CN109133104B (en) | A process, system and application for co-production of synthetic ammonia from blue carbon tail gas and calcium carbide tail gas | |
| CN113148953B (en) | System and method for preparing ethylene glycol from synthesis gas | |
| CN203668330U (en) | Device for drying, purifying and cooling reformed synthesis gas and SNC (Synthetic Natural Gas) product gas by using low temperature methanol washing | |
| CN106178839A (en) | Method for recovering and extracting hydrogen and light hydrocarbon in hydrogen-containing rich gas | |
| CN221906416U (en) | Gas purifying device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |