CN107694292B - Regeneration method of semi-lean absorbent - Google Patents
Regeneration method of semi-lean absorbent Download PDFInfo
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- CN107694292B CN107694292B CN201711031329.4A CN201711031329A CN107694292B CN 107694292 B CN107694292 B CN 107694292B CN 201711031329 A CN201711031329 A CN 201711031329A CN 107694292 B CN107694292 B CN 107694292B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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Abstract
The invention relates to a regeneration method of a semi-lean absorbent, which is provided with four-stage flash evaporation operation and can effectively reduce CO in the semi-lean absorbent2The content of the semi-lean absorbent is increased, the absorption capacity of the semi-lean absorbent is improved, the circulation quantity of the semi-lean absorbent is reduced, and the energy consumption of a system is further reduced; particularly, a compressor and an ejector are arranged in a connecting pipeline of the four-stage flash device, so that the four flash tanks can carry out flash evaporation at different pressure levels. In addition, the three-level flash tank and the four-level flash tank share the same tank body, and two times of flash evaporation can be effectively realized in one tank body by oppositely arranging partition plates in the tank body, so that the arrangement structure is simple, the number of equipment is reduced, the occupied area is saved, and the construction difficulty is reduced.
Description
Technical Field
The invention relates to the technical field of chemical processes, in particular to a regeneration method of a semi-lean absorbent.
Background
The synthesis gas purification is mainly used for removing H in the crude synthesis gas2S、COS、CO2Thereby producing a purified gas satisfying the process requirements. The synthesis gas purification processes commonly used in industry are generally classified into a hot process and a cold process according to the difference of absorption temperature. Selexol and MDEA processes are best known in the hot process, and the cold process is lowA warm methanol wash is representative. The three typical synthetic gas purification technologies have the characteristics of high purification degree, good selectivity, low energy consumption and the like, and are widely applied to various large coal gasification devices.
Through the wide industrial application in recent years, the processes such as Selexol, MDEA and low-temperature methanol washing can reach an advanced level on the index of acid gas purification, but the optimization of energy consumption needs to be further improved, and the method of setting the semi-lean absorbent for recycling as the inlet absorbent of the absorption tower can reduce the circulation amount of the absorbent of the system and reduce the overall energy consumption.
After the regeneration and use process of the semi-lean absorbent is developed, the energy consumption of the synthesis gas purification process is greatly reduced, and the semi-lean absorbent is not completely regenerated in the solution regeneration process and carries certain CO2The absorbent solution is fed directly to the absorber tower as an auxiliary absorbent for the fully regenerated lean absorbent. Due to the semi-lean absorbent as absorbent, in which CO is present2The lower the content of (A), the better the absorption capacity and the lower the energy consumption of the whole system. The existing synthesis gas purification technology still has the defect of high energy consumption, and needs to improve the regeneration process of the semi-lean absorbent, so as to reduce the cold quantity of the system and the circulation quantity of the absorbent, thereby reducing the energy consumption.
Disclosure of Invention
The invention aims to solve the technical problem of providing a method for effectively reducing CO in a semi-lean absorbent aiming at the current situation of the prior art2Content, thereby reducing the energy consumption of the system and reducing the circulating amount of the absorbent.
The technical scheme adopted by the invention for solving the technical problems is as follows: a method of regenerating a semi-lean absorbent, characterized by comprising the steps of:
enabling the carbon-rich absorbent from the upstream to enter a primary flash tank for flash evaporation at a temperature of-10 to-55 ℃ and a pressure of 0.3 to 4.2MPaG, wherein the flash evaporation temperature of the primary flash tank is-20 to-65 ℃ and the flash evaporation pressure of the primary flash tank is 0.07 to 2.0MPaG, introducing a liquid phase subjected to flash evaporation into a secondary flash tank, and introducing a gas phase subjected to flash evaporation by the primary flash tank into the secondary flash tank through an ejector;
the flash temperature of the secondary flash tank is-25 to-70 ℃, the flash pressure is 0.02 to 1.8MPaG, the liquid phase after flash evaporation is divided into a first liquid phase flow and a second liquid phase flow, and the flow ratio of the first liquid phase flow to the second liquid phase flow is 1:9 to 9: 1; the first liquid phase stream is introduced into a three-stage flash drum, and the second liquid phase stream is introduced into a stripper; the top of the secondary flash tank is provided with a gas phase outlet, and flash gas in the secondary flash tank is sent to the downstream through the gas phase outlet;
the flash temperature of the third-level flash tank is-30 to-80 ℃, the flash pressure is-0.09 to 0.4MPaG, the liquid phase after flash evaporation is led into the fourth-level flash tank, and the gas phase generated by flash evaporation of the third-level flash tank is led into the second-level flash tank;
the flash temperature of the four-level flash tank is-30 to-80 ℃, the flash pressure is-0.09 to 0.4MPaG, and CO in the liquid phase after flash evaporation2The molar concentration of the semi-lean absorbent is 2-15%, the temperature is-30 to-80 ℃, and the semi-lean absorbent is sent to upstream for recycling; the gas phase generated by the four-stage flash drum is divided into a first gas-phase flow and a second gas-phase flow, the first gas-phase flow is guided into the secondary flash drum through the ejector, the second gas-phase flow is guided into the secondary flash drum through the compressor, and an outlet of the ejector is communicated with an outlet of the compressor, so that the first gas-phase flow and the second gas-phase flow are combined and then are sent to the secondary flash drum;
enabling the sulfur-rich absorbent from the upstream to have the temperature of-10 to-55 ℃ and the pressure of 0.3 to 4.2MPaG, entering the stripping tower for stripping operation, introducing stripping gas, preferably nitrogen, into the lower part of the stripping tower, and enabling the operating temperature of the stripping tower to be-25 to-80 ℃ and the operating pressure of the stripping tower to be-0.09 to 0.1 MPaG; and conveying the sulfur-rich absorbent stripped by the stripper to the downstream, and outputting a gas phase generated after stripping by the stripper as tail gas.
Preferably, the upper part of the primary flash tank is communicated with a first liquid inlet pipeline used for conveying the carbon-rich absorbent from upstream, the top of the primary flash tank is provided with a first gas outlet used for connecting a first inlet of an ejector, and a liquid phase outlet at the bottom of the primary flash tank is communicated with the upper part of the secondary flash tank;
the top of the secondary flash tank is connected with CO conveying2A first gas outlet pipeline of the product gas, wherein a liquid phase outlet of the secondary flash tank is connected with a liquid outlet pipeline, the liquid outlet pipeline is divided into a first liquid outlet pipeline and a second liquid outlet pipeline, the first liquid outlet pipeline is connected with the tertiary flash tank through a heat exchanger, the second liquid outlet pipeline is connected with the gas stripping tower, the first liquid phase stream is conveyed through the first liquid outlet pipeline, and the second liquid phase stream is conveyed through the second liquid outlet pipeline;
the top of the third-stage flash tank is connected with a second gas outlet pipeline for conveying flash gas to the second-stage flash tank; a liquid phase outlet at the bottom of the third-stage flash tank is communicated with the upper part of the fourth-stage flash tank;
the top of the four-level flash tank is connected with an air outlet pipeline which is divided into a third air outlet pipeline and a fourth air outlet pipeline, the first gas-phase flow is conveyed through the third air outlet pipeline, the second gas-phase flow is conveyed through the fourth air outlet pipeline, the third air outlet pipeline is connected with a second inlet of the ejector, the fourth air outlet pipeline is connected with an inlet of the compressor, and an outlet of the ejector and an outlet of the compressor are communicated with the two-level flash tank; the bottom of the four-stage flash tank is connected with a third liquid outlet pipeline for conveying the semi-lean absorbent;
the upper part of the gas stripping tower is communicated with a second liquid inlet pipeline used for conveying the sulfur-rich absorbent from upstream, the top of the gas stripping tower is connected with a fifth gas outlet pipeline used for conveying tail gas, the lower part of the gas stripping tower is connected with a gas inlet pipeline used for conveying gas stripping gas, and the bottom of the gas stripping tower is connected with a fourth liquid outlet pipeline used for outputting the sulfur-rich absorbent.
As an improvement, the secondary flash tank is divided into two sections which are arranged up and down, and the two sections are separated by a first liquid collecting tray provided with an air lifting cap; the liquid phase output from the bottom of the primary flash tank is guided into the upper part of the upper section of the secondary flash tank; the liquid phase output from the bottom of the upper section of the secondary flash tank is divided into the first liquid phase stream and the second liquid phase stream, and the liquid phase output from the bottom of the lower section of the secondary flash tank is introduced into the stripper; introducing the gas phase flashed by the third-level flash tank into the upper part of the lower end of the second-level flash tank; an outlet of the ejector and an outlet of the compressor communicate with an upper portion of a lower section of the secondary flash tank.
The carbon-rich absorbent from the upstream is divided into a third liquid phase stream and a fourth liquid phase stream, the flow ratio of the third liquid phase stream to the fourth liquid phase stream is 1: 9-9: 1, the third liquid phase stream is introduced into the primary flash tank, and the fourth liquid phase stream is introduced into the upper part of the lower section of the secondary flash tank; dividing a sulfur-rich absorbent from the upstream into a fifth liquid phase stream and a sixth liquid phase stream, wherein the flow ratio of the fifth liquid phase stream to the sixth liquid phase stream is 1: 50-50: 1, the fifth liquid phase stream is introduced into the stripper, and the sixth liquid phase stream is introduced into the upper part of the lower section of the secondary flash tank; the stripping nitrogen is divided into a third gas-phase flow and a fourth gas-phase flow, and the flow ratio of the third gas-phase flow to the fourth gas-phase flow is 1: 0-20: 1; the third vapor phase stream is directed to the stripper and the fourth vapor phase stream is directed to the four-stage flash drum. The carbon-rich absorbent and the sulfur-rich absorbent from the upstream are respectively split and enter the lower part of a secondary flash drum for flash evaporation, and on one hand, CO in the sulfur-rich absorbent can be enabled to be evaporated2Desorbing gas to increase CO2The yield of the product gas; on the other hand, the carbon-rich absorbent entering from the upper part can wash flash steam of the sulfur-rich absorbent to absorb resolved H2S gas, CO increase2The purity of the product gas. In addition, a small amount of nitrogen is introduced into the four-stage flash tank, so that the regeneration of the semi-lean liquid absorbent can be more sufficient, and the CO in the semi-lean liquid absorbent is reduced2But to some extent reduces the CO content2The purity of the product gas can be adjusted to N according to the production requirement2And selecting whether the strands are divided into four flash tanks preferentially.
As an improvement, the three-stage flash tank and the four-stage flash tank share the same tank body, and a flash baffle and an overflow baffle are arranged in the tank body; the lower end edge of the flash evaporation partition plate is suspended, the rest of the peripheries are connected with the inner wall of the tank body, the upper end edge of the overflow partition plate is suspended, the rest of the peripheries are connected with the inner wall of the tank body, the suspended end of the flash evaporation partition plate and the suspended end of the overflow partition plate are partially overlapped in the vertical direction, a gap is reserved between the overlapped parts, the inner cavity of the tank body is divided into a first cavity and a second cavity, the two cavities are communicated through the gap between the flash evaporation partition plate and the overflow partition plate, the first cavity is the three-stage flash tank, and the second cavity is the four-stage flash tank.
The first-stage flash tank, the second-stage flash tank, the third-stage flash tank, the fourth-stage flash tank and the stripping tower share the same tower body, the tower body is sequentially divided into seven sections from top to bottom, wherein the first section is the first-stage flash tank, the second and third sections are the second-stage flash tanks, the fourth section is a combined tank body shared by the third-stage flash tank and the fourth-stage flash tank, and the V section, the VI section and the VII section are the stripping tower; the second-stage flash tank is characterized in that the second section and the third section of the second-stage flash tank are isolated by a first liquid collecting tray provided with an air lifting cap, the fourth section of the combined tank body is isolated by a first end enclosure, the V section and the VI section of the gas stripping tower are isolated by a second liquid collecting tray provided with an air lifting cap, the VI section and the VII section of the gas stripping tower are isolated by a third liquid collecting tray provided with an air lifting cap, the bottom of the V section of the gas stripping tower is connected with the upper part of the VI section of the gas stripping tower through a first circulating pump, and the bottom of the VI section of the gas stripping tower is connected with the upper part of the VII section of the gas stripping tower through a second circulating pump.
Or the first-stage flash tank, the second-stage flash tank and the stripping tower share the same tower body, and the tower body is sequentially divided into six sections from top to bottom, wherein the first section is the first-stage flash tank, the second section and the third section are the second-stage flash tanks, and the V section, the VI section and the VII section are the stripping towers; the second-stage flash tank is isolated from the third-stage flash tank by a first liquid collecting tray provided with an air lifting cap, the third-stage flash tank is isolated from the V-stage flash tank by a second end enclosure, the V-stage flash tank is isolated from the VI-stage flash tank by a second liquid collecting tray provided with an air lifting cap, the VI-stage flash tank is isolated from the VII-stage flash tank by a third liquid collecting tray provided with an air lifting cap, the bottom of the V-stage flash tank is connected with the upper part of the VI-stage flash tank by a first circulating pump, the bottom of the VI-stage flash tank is connected with the upper part of the VII-stage flash tank by a second circulating pump, and the third-stage flash tank is independently arranged with a combined tank shared by the fourth-stage flash tank.
Or the gas stripping tower is divided into three sections, namely a V section, a VI section and a VII section, wherein the VI section and the VII section which are arranged up and down share a first tower body, the V section of the gas stripping tower shares a second tower body with the first-stage flash tank, the second-stage flash tank, the third-stage flash tank and the fourth-stage flash tank, the second tower body is sequentially divided into five sections from top to bottom, wherein the first section is the first-stage flash tank, the second section and the third section are the second-stage flash tank, the second section and the third section of the second-stage flash tank are isolated by a first liquid collecting tray provided with an air lifting cap, and the IV section is a combined tank body shared by the third-stage flash tank and the fourth-stage flash tank; the combined tank body is isolated from the section V of the stripping tower through a first seal head, the section VI and the section VII of the stripping tower are isolated through a third liquid collecting tray provided with a gas lifting cap, the bottom of the section V of the stripping tower is connected with the upper part of the section VI of the stripping tower through a first circulating pump, and the bottom of the section VI of the stripping tower is connected with the upper part of the section VII of the stripping tower through a second circulating pump.
Or the gas stripping tower is divided into three sections, namely a V section, a VI section and a VII section, wherein the VI section and the VII section which are arranged up and down share the first tower body, the V section of the gas stripping tower, the first-stage flash tank and the second-stage flash tank share the second tower body, and the second tower body is sequentially divided into four sections from top to bottom, wherein the first section is the first-stage flash tank, and the second section and the third section are the second-stage flash tank; the second-stage flash tank is characterized in that a second section II and a third section III are isolated by a first liquid collecting tray provided with a gas lifting cap, a third section III of the second-stage flash tank is isolated by a second end enclosure, a section VI and a section VII of the gas stripping tower are isolated by a third liquid collecting tray provided with a gas lifting cap, the bottom of the section V of the gas stripping tower is connected with the upper part of the section VI of the gas stripping tower through a first circulating pump, the bottom of the section VI of the gas stripping tower is connected with the upper part of the section VII of the gas stripping tower through a second circulating pump, and the third-stage flash tank and the combined tank shared by the fourth-stage flash tanks are independently arranged.
Compared with the prior art, the invention has the advantages that: the four-stage flash evaporation operation is arranged in the regeneration method of the semi-lean absorbent, so that the CO in the semi-lean absorbent can be effectively reduced2The content of the semi-lean absorbent improves the absorption capacity of the semi-lean absorbent, reduces the circulation amount of the semi-lean absorbent and further reduces the energy consumption of a system; particularly, the compressor and the ejector are arranged in a connecting pipeline of the four-level flash evaporation operation, so that the four flash tanks can carry out flash evaporation of different pressure levels, wherein under the suction action of the compressor and the ejector, the four-level flash tanks can reach a negative pressure state, the regeneration effect of the semi-lean absorbent is obviously improved, the load of the compressor can be reduced to a certain extent by matching the ejector, the energy consumption is reduced, in addition, the three-level flash tanks and the four-level flash tanks share the same tank body, and the flash baffles and the overflow baffles are oppositely arranged in the tank body, so that the two-time flash evaporation can be effectively realized in one tank body.
The invention is particularly suitable for being used in a matched gas purification process and is used for regenerating an absorbent used in the gas purification process.
Drawings
FIG. 1 is a schematic view of example 1 of the present invention;
FIG. 2 is a schematic view of example 2 of the present invention;
FIG. 3 is a schematic view of example 3 of the present invention;
fig. 4 is a schematic view of embodiment 4 of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
The gases treated in the following examples are all CO-rich gases from an upstream gas production plant2And H2Non-purified gas of acid gas such as S, etc. with main gas composition of H275-8 percent of CO, 75-0.1 percent of CO2Content 60% -2%, H2The S content is 5-0.0001%, and the used absorbent can be Selexol, NHD, MDEA, methanol and other physical absorbents.
Examples 1,
The regeneration method of the semi-lean absorbent as shown in fig. 1, wherein the temperature of the carbon-rich absorbent from the upstream is-20 to-45 ℃, the pressure is 1.5 to 3.0MPaG, the carbon-rich absorbent is divided into two streams of a third liquid phase stream and a fourth liquid phase stream, the third liquid phase stream enters a primary flash tank 1, the fourth liquid phase stream is introduced to the upper part of the section iii of a secondary flash tank 2, and the flow ratio of the third liquid phase stream to the fourth liquid phase stream is 1:9 to 9: 1; correspondingly, a first liquid inlet pipeline for conveying the carbon-rich absorbent from the upstream is divided into a first branch and a second branch, the first branch is communicated with the upper part of the first-stage flash tank 1 and is used for conveying a third liquid phase stream, and the second branch is communicated with the upper part of the III section of the second-stage flash tank 2 and is used for conveying a fourth liquid phase stream;
when the primary flash tank 1 is subjected to flash evaporation operation, the flash evaporation temperature is-30 to-55 ℃, the flash evaporation pressure is 0.10 to 1.5MPaG, the liquid phase subjected to flash evaporation is introduced into the upper part of the second section of the secondary flash tank 2, and the gas phase subjected to flash evaporation by the primary flash tank 1 is introduced into the upper part of the third section of the secondary flash tank 2 through the first inlet of the ejector 6; wherein, the top of one-level flash tank 1 is equipped with the first gas outlet of output flash steam, is equipped with pressure detection adjusting device 13a between the first gas outlet of ejector 6 and one-level flash tank 1, under the operating mode of difference, can adjust the operating pressure of ejector 6 in a flexible way, and CO in the absorbent of more effectual reduction half poverty2The concentration of (c).
The flash temperature of the secondary flash tank 2 is-35 to-60 ℃, the flash pressure is 0.2 to 1.5MPaG, the liquid phase after flash evaporation is divided into a first liquid phase flow and a second liquid phase flow, and the flow ratio of the first liquid phase flow to the second liquid phase flow is that1: 9-9: 1; the top of the second stage of the two-stage flash tank 2 is connected with CO transportation2The first gas outlet pipeline of the product gas takes the flash gas in the secondary flash tank 2 (including flash gas which is flash evaporated by other flash tanks and then is guided into the secondary flash tank 2) as CO2The product gas is sent to the downstream; a liquid phase outlet at the lower part of the second section of the secondary flash tank 2 is connected with a liquid outlet pipeline, and the liquid outlet pipeline is divided into a first liquid outlet pipeline and a second liquid outlet pipeline, wherein a first liquid phase stream is conveyed through the first liquid outlet pipeline, and a second liquid phase stream is conveyed through the second liquid outlet pipeline; the first liquid phase flow strand is subjected to heat exchange by a heat exchanger 14 and heated to-25 to-45 ℃, and then is guided into the upper part of a three-stage flash tank 3, and the second liquid phase flow strand is guided into the upper part of a V section of a stripping tower 5.
The flash temperature of a third-level flash tank (cavity) 3 in the combined tank body is-40 to-70 ℃, the flash pressure is-0.05 to 0.3MPaG, the flash liquid phase overflows into a fourth-level flash tank (cavity) 4 through a gap between a flash partition plate 32 and an overflow partition plate 42, and the gas phase flash evaporated by the third-level flash tank (cavity) 3 is conveyed to the upper part of a section III of the second-level flash tank 2 through a second gas outlet pipeline arranged at the top of the gas phase flash tank;
the flash temperature of a four-level flash tank (cavity) 4 in the combined tank body is-40 to-70 ℃, the flash pressure is-0.05 to 0.3MPaG, and CO in the flash liquid phase2The molar concentration of the semi-lean absorbent is 3-5%, the temperature is-30 to-80 ℃, and the semi-lean absorbent is sent to upstream for recycling; the gas phase flashed in the four-stage flash tank (chamber) 4 is divided into a first gas phase stream and a second gas phase stream, the first gas phase stream is introduced into the upper part of the section iii of the two-stage flash tank 2 through the ejector 6, and the second gas phase stream is introduced into the upper part of the section iii of the two-stage flash tank 2 through the compressor 7. The top of the four-level flash tank (cavity) 4 is connected with an air outlet pipeline which is divided into a third air outlet pipeline and a fourth air outlet pipeline, a first gas phase stream is conveyed through the third air outlet pipeline, and a second gas phase stream is conveyed through the fourth air outlet pipeline; the third gas outlet pipeline is connected with the second inlet of the ejector 6, the fourth gas outlet pipeline is connected with the inlet of the compressor 7, the outlet of the ejector 6 and the outlet of the compressor 7 are communicated with the upper part of the III section of the two-stage flash tank 2, so that the first gas-phase flow and the second gas-phase flow are combined and then are sent to the ejectorThe secondary flash tank 2; a pressure detection and adjustment device 13b is further arranged in a fourth gas outlet pipeline where the second gas phase flow is located, so that the operating pressure of the compressor 7 can be flexibly adjusted under different working conditions, the operating flexibility of the four-stage flash tank (cavity) 4 is improved, and the CO in the semi-lean absorbent is more effectively reduced2The concentration of (c); the bottom of the four-stage flash tank (cavity) 4 is connected with a third liquid outlet pipeline for conveying the semi-lean absorbent, a fourth circulating pump 11 is arranged in the third liquid outlet pipeline, and the semi-lean absorbent is pressurized by the fourth circulating pump 11 and then is sent to the downstream.
The temperature of a sulfur-rich absorbent from upstream is-20 to-45 ℃, the pressure is 1.5 to 3.0MPaG, the sulfur-rich absorbent is divided into a fifth liquid phase stream and a sixth liquid phase stream, and the flow ratio of the fifth liquid phase stream to the sixth liquid phase stream is 1:50 to 50: 1; correspondingly, a second liquid inlet pipeline for conveying the sulfur-rich absorbent from the upstream is divided into a third branch and a fourth branch; the third branch is communicated with the upper part of the section III of the secondary flash tank 2 and is used for conveying a sixth liquid phase stream, and the fourth branch is communicated with the upper part of the section V of the stripping tower 5 and is used for conveying a fifth liquid phase stream; the liquid inlet position of a sixth liquid phase stream for conveying the sulfur-rich absorbent connected to the upper part of the section III of the flash tank 2 is lower than that of a fourth liquid phase stream for conveying the carbon-rich absorbent connected to the upper part of the section III of the flash tank 2, so that the carbon-rich absorbent can spray and wash flash steam of the sulfur-rich absorbent at the lower part, and H in the flash steam is reduced2S content, increase of CO2The purity of the product gas.
The operating temperature of the stripper column 5 is-35 to-70 ℃, and the operating pressure is-0.09 to 0.1 MPaG; the stripping gas can be divided into a third gas-phase stream and a fourth gas-phase stream, and the flow ratio of the third gas-phase stream to the fourth gas-phase stream is 1: 0.001-20: 1; the third gas phase flow is guided into the lower part of the VII section of the gas stripping tower 5, the fourth gas phase flow is guided into the lower part of the four-stage flash drum (cavity) 4, and the stripping gas is guided through a gas inlet pipeline at the lower part of the VII section of the gas stripping tower 5, wherein the stripping gas is preferably N2The bottom of the VII section of the gas stripping tower 5 is also connected with a fourth liquid outlet pipeline for outputting the sulfur-rich absorbent, and a third circulating pump 10 is also arranged in the fourth liquid outlet pipeline for rich sulfurThe absorbent is pressurized and then sent to the downstream; after the sulfur-rich absorbent is subjected to gas stripping in the gas stripping tower 5, CO in the sulfur-rich absorbent is reduced2Thereby relatively increasing H2And the concentration of S is outputted by a fifth gas outlet pipeline at the top of the V section of the stripping tower 5 as tail gas after the gas phase is stripped by the stripping tower 5.
The tower body is sequentially divided into seven sections from top to bottom, wherein the first section is the first-stage flash tank 1, the second-stage flash tank 2, the third-stage flash tank 3, the fourth-stage flash tank 4 and the stripper column 5 share the same tower body structure, the first section is the first-stage flash tank 1, the second section and the third section are the second-stage flash tank 2, the fourth section is a combined tank body of the third-stage flash tank 3 and the fourth-stage flash tank 4, and the V section, the VI section and the VII section are the stripper column 5; wherein, a flash evaporation clapboard 32 and an overflow clapboard 42 are arranged in the combined tank body of the IV section; the lower end edge of the flash separation plate 32 is suspended, the rest of the periphery is connected with the inner wall of the tank body, the upper end edge of the overflow separation plate 42 is suspended, the rest of the periphery is connected with the inner wall of the tank body, the suspended end of the flash separation plate 32 and the suspended end of the overflow separation plate 42 are partially overlapped in the vertical direction, a gap is reserved between the overlapped parts, the inner cavity of the tank body is divided into a first cavity and a second cavity, the two cavities are communicated through the gap between the flash separation plate 32 and the overflow separation plate 42, the first cavity is the three-level flash tank (cavity) 3, and the second cavity is the four-level flash tank (cavity) 4. The second section and the third section of the second-stage flash tank 2 are separated by a first liquid collecting tray 21 provided with an air lifting cap, the combined tank body of the fourth section is separated from the V section of the stripping tower 5 by a first end enclosure 31, the V section and the VI section of the stripping tower 5 are separated by a second liquid collecting tray 51 provided with an air lifting cap, the VI section and the VII section of the stripping tower 5 are separated by a third liquid collecting tray 52 provided with an air lifting cap, the bottom of the V section of the stripping tower 5 is connected with the upper part of the VI section of the stripping tower 5 by a first circulating pump 8, and the bottom of the VI section of the stripping tower 5 is connected with the upper part of the VII section of the stripping tower 5 by a second circulating pump 9. In addition, the bottom of the section V of the stripping tower 5 is provided with a liquid level detection control device 12a, the bottom of the section VI is provided with a liquid level detection control device 12b, and the bottom of the section VII is provided with a liquid level detection control device 12c for controlling the liquid level in the stripping tower 5.
Example 2
In the method for regenerating a semi-lean absorbent as shown in fig. 2, this embodiment is different from embodiment 1 in that the first-stage flash tank 1, the second-stage flash tank 2 and the stripping column 5 share the same column body, and the column body is divided into six sections in sequence from top to bottom, where the first section is the first-stage flash tank 1, the second and third sections are the second-stage flash tanks 2, and the sections v, vi and vii are the stripping column 5; the three-stage flash tank 3 and the four-stage flash tank 4 share the same tank, which is separately arranged outside the column and has the same structure as that of example 1. The second section and the third section of the second-stage flash tank 2 are separated by a first liquid collecting tray 21 provided with an air lifting cap, the third section of the second-stage flash tank 2 is separated by a second end enclosure from the V section of the stripping tower 5, the V section and the VI section of the stripping tower 5 are separated by a second liquid collecting tray 51 provided with an air lifting cap, the VI section and the VII section of the stripping tower 5 are separated by a third liquid collecting tray 52 provided with an air lifting cap, the bottom of the V section of the stripping tower 5 is connected with the upper part of the VI section of the stripping tower 5 by a first circulating pump 8, and the bottom of the VI section of the stripping tower 5 is connected with the upper part of the VII section of the stripping tower 5 by a second circulating pump 9. Otherwise, the rest of the present embodiment is the same as embodiment 1, and will not be repeated.
Examples 3,
The method for regenerating a semi-lean absorbent as shown in fig. 3 is different from example 1 in that the stripper 5 is divided into three sections, namely a V section, a vi section and a vii section, wherein the vi section and the vii section which are arranged up and down share a first tower body, the V section of the stripper shares a second tower body with the first-stage flash tank 1, the second-stage flash tank 2, the third-stage flash tank 3 and the fourth-stage flash tank 4, and the second tower body is divided into five sections from top to bottom, wherein the first section is the first-stage flash tank 1, the second section and the third section are the second-stage flash tank 2, and the iv section is a combined tank body shared by the third-stage flash tank 3 and the fourth-stage flash tank 4, and the tank body has the same structure as that in example 1. The second section and the third section of the second-stage flash tank 2 are isolated by a first liquid collecting tray 21 provided with a gas lifting cap, the combined tank body of the fourth section is isolated by a first seal head 31 with the V section of the gas stripping tower 5, the gas phase outlet at the top of the VI section of the gas stripping tower 5 is communicated with the bottom of the V section of the gas stripping tower 5 through an external pipeline, the liquid phase outlet at the bottom of the V section of the gas stripping tower 5 is connected with the upper part of the VI section of the gas stripping tower 5 through a first circulating pump 8, a third liquid collecting tray 52 provided with a gas lifting cap is adopted between the VI section and the VII section of the gas stripping tower 5, and the bottom of the VI section of the gas stripping tower 5 is connected with the upper part of the VII section of the gas stripping tower 5 through a second circulating pump 9. Otherwise, the rest of the present embodiment is the same as embodiment 1, and will not be repeated.
Examples 4,
In the method for regenerating a semi-lean absorbent as shown in fig. 4, this embodiment is different from embodiment 1 in that the stripper 5 is divided into three sections, namely a V section, a vi section and a vii section, wherein the vi section and the vii section which are arranged up and down share a first tower body, the V section of the stripper shares a second tower body with a first-stage flash tank 1 and a second-stage flash tank 2, and the second tower body is sequentially divided into four sections from top to bottom, wherein the first section is the first-stage flash tank 1, and the second section and the third section are the second-stage flash tank 2; the three-stage flash tank 3 and the four-stage flash tank 4 share the same tank, which is separately provided outside the column and has the same configuration as in example 1. The second section and the third section of the second-stage flash tank 2 are isolated by a first liquid collecting tray 21 provided with a gas lifting cap, the third section of the second-stage flash tank 2 is isolated from the V section of the gas stripping tower 5 by a second end enclosure 22, a gas phase outlet at the top of the VI section of the gas stripping tower 5 is communicated with the bottom of the V section of the gas stripping tower 5 by an external pipeline, a liquid phase outlet at the bottom of the V section of the gas stripping tower 5 is connected with the upper part of the VI section of the gas stripping tower 5 by a first circulating pump 8, a third liquid collecting tray 52 provided with a gas lifting cap is adopted between the VI section and the VII section of the gas stripping tower 5 for isolation, and the bottom of the VI section of the gas stripping tower 5 is connected with the upper part of the VII section of the gas stripping tower 5 by a second circulating pump 9. Otherwise, the rest of the present embodiment is the same as embodiment 1, and will not be repeated.
Compared with the effect of the conventional process in the prior art, the CO which is obtained by adopting the regeneration method of the semi-lean absorbent and the carbon-rich absorbent subjected to four-stage flash evaporation as the semi-lean absorbent by adopting the regeneration method of the semi-lean absorbent2The molar content of the compound is lower and can reach 2-15%, and the preferable process configurationCan make CO in semi-lean absorbent2The molar content reaches 3-5%, and the temperature of the semi-poor absorbent is lower and is close to-70 ℃; taking 4.0MPaG gasification matched low-temperature methanol washing as an example, compared with the conventional process, the absorption capacity of the semi-lean absorbent is improved by about 80 percent, and the using amount of the semi-lean absorbent is reduced by about 44 percent; for 6.5MPaG gasification matched low-temperature methanol washing, the absorption capacity of the semi-lean absorbent is improved by about 2 times, and the using amount of the semi-lean absorbent is reduced by about 66%; in addition, the regeneration method of the semi-lean absorbent can reduce the cold consumption of the system by 20-40%.
In conclusion, the four-stage flash evaporation operation is arranged in the regeneration method of the semi-lean absorbent, so that the CO in the semi-lean absorbent can be effectively reduced2The content of the semi-lean absorbent is increased, the absorption capacity of the semi-lean absorbent is improved, the circulation quantity of the semi-lean absorbent is reduced, and the energy consumption of a system is further reduced; particularly, the compressor 7 and the ejector 6 are arranged in the connecting pipeline of the four-stage flash device, so that the four flash tanks can carry out flash evaporation at different pressure levels, wherein under the suction action of the compressor 7 and the ejector 6, the four-stage flash tank 4 can reach a negative pressure state, and the regeneration effect of the semi-lean absorbent is obviously improved. In addition, the three-level flash tank 3 and the four-level flash tank 4 share the same tank body, and two times of flash evaporation can be effectively realized in one tank body by oppositely arranging the flash partition plate 32 and the overflow partition plate 42 in the tank body, so that the arrangement structure is simple, the number of flash evaporation equipment is reduced, the occupied area is saved, and the construction difficulty is reduced.
Claims (8)
1. A method of regenerating a semi-lean absorbent, characterized by comprising the steps of:
enabling the carbon-rich absorbent from the upstream to enter a primary flash tank (1) for flash operation at a temperature of-10 to-55 ℃ and a pressure of 0.3 to 4.2MPaG, enabling a flash temperature of the primary flash tank (1) to be-20 to-65 ℃ and a flash pressure of 0.07 to 2.0MPaG, introducing a liquid phase subjected to flash operation into a secondary flash tank (2), and introducing a gas phase subjected to flash operation through the primary flash tank (1) into the secondary flash tank (2) through an ejector (6);
the flash temperature of the secondary flash tank (2) is-25 to-70 ℃, the flash pressure is 0.02 to 1.8MPaG, the liquid phase after flash evaporation is divided into a first liquid phase flow and a second liquid phase flow, and the flow ratio of the first liquid phase flow to the second liquid phase flow is 1:9 to 9: 1; the first liquid phase stream is directed to a three-stage flash drum (3) and the second liquid phase stream is directed to a stripper; the top of the secondary flash tank (2) is provided with a gas phase outlet, and flash gas in the secondary flash tank (2) is sent to the downstream through the gas phase outlet;
the flash temperature of the third-level flash tank (3) is-30 to-80 ℃, the flash pressure is-0.09 to 0.4MPaG, the liquid phase after flash evaporation is led into the fourth-level flash tank (4), and the gas phase after flash evaporation by the third-level flash tank (3) is led into the second-level flash tank (2);
the flash temperature of the four-level flash tank (4) is-30 to-80 ℃, the flash pressure is-0.09 to 0.4MPaG, and CO in the liquid phase after the four-level flash is carried out2The molar concentration of the semi-lean absorbent is 2-15%, the temperature is-30 to-80 ℃, and the semi-lean absorbent is sent to the upstream as the semi-lean absorbent; the gas phase flashed by the four-stage flash drum (4) is divided into a first gas phase stream and a second gas phase stream, the first gas phase stream is introduced into the two-stage flash drum (2) through the ejector (6), the second gas phase stream is introduced into the two-stage flash drum (2) through a compressor (7), wherein an outlet of the ejector (6) is communicated with an outlet of the compressor (7);
enabling the sulfur-rich absorbent from the upstream to have the temperature of-10 to-55 ℃ and the pressure of 0.3 to 4.2MPaG, entering the stripping tower (5) for stripping operation, introducing stripping nitrogen into the lower part of the stripping tower (5), and enabling the operating temperature of the stripping tower (5) to be-25 to-80 ℃ and the operating pressure of-0.09 to 0.1 MPaG; the sulfur-rich absorbent stripped by the stripper (5) is sent to the downstream, and the gas phase stripped by the stripper (5) is sent to the downstream as tail gas;
the upper part of the primary flash tank (1) is communicated with a first liquid inlet pipeline used for conveying a carbon-rich absorbent from upstream, the top of the primary flash tank (1) is provided with a first gas outlet used for connecting a first inlet of an ejector (6), and a liquid phase outlet at the bottom of the primary flash tank (1) is communicated with the upper part of the secondary flash tank (2);
said second stageThe top of the flash tank (2) is connected with CO transportation2A first gas outlet pipeline of the product gas, wherein a liquid phase outlet of the secondary flash tank (2) is connected with a liquid outlet pipeline which is divided into a first liquid outlet pipeline and a second liquid outlet pipeline, the first liquid outlet pipeline is connected with the third-stage flash tank (3) through a heat exchanger (14), and the second liquid outlet pipeline is connected with the stripper (5); wherein the first liquid phase stream is delivered through the first outlet conduit and the second liquid phase stream is delivered through the second outlet conduit;
the top of the third-level flash tank (3) is connected with a second gas outlet pipeline for conveying flash gas to the second-level flash tank (2); a liquid phase outlet at the bottom of the three-stage flash tank (3) is communicated with the upper part of the four-stage flash tank (4);
the top of the four-level flash tank (4) is connected with an air outlet pipeline, the air outlet pipeline is divided into a third air outlet pipeline and a fourth air outlet pipeline, the first gas-phase flow is conveyed through the third air outlet pipeline, the second gas-phase flow is conveyed through the fourth air outlet pipeline, the third air outlet pipeline is connected with the second inlet of the ejector (6), the fourth air outlet pipeline is connected with the inlet of the compressor (7), and the outlet of the ejector (6) and the outlet of the compressor (7) are communicated with the secondary flash tank (2); the bottom of the four-stage flash tank (4) is connected with a third liquid outlet pipeline for conveying a semi-lean absorbent;
the upper part of the gas stripping tower (5) is communicated with a second liquid inlet pipeline used for conveying the sulfur-rich absorbent from the upstream, the top of the gas stripping tower (5) is connected with a fifth gas outlet pipeline used for conveying tail gas, the lower part of the gas stripping tower (5) is connected with a gas inlet pipeline used for conveying stripping gas, and the bottom of the gas stripping tower (5) is connected with a fourth liquid outlet pipeline used for outputting the sulfur-rich absorbent.
2. The semi-lean absorbent regeneration method of claim 1, characterized in that: the secondary flash tank (2) is divided into two sections which are arranged up and down, and the two sections are separated by a first liquid collecting tray (21) provided with an air lifting cap; the liquid phase at the bottom of the primary flash tank (1) is introduced to the upper part of the upper section of the secondary flash tank (2); the liquid phase output from the bottom of the upper section of the secondary flash drum (2) is divided into the first liquid phase stream and the second liquid phase stream, and the liquid phase output from the bottom of the lower section of the secondary flash drum (2) is introduced into the stripper (5); introducing the gas phase flashed by the third-level flash tank (3) into the upper part of the lower section of the second-level flash tank (2); the outlet of the ejector (6) and the outlet of the compressor (7) are communicated with the upper part of the lower section of the secondary flash tank (2).
3. The semi-lean absorbent regeneration method of claim 2, characterized in that: the carbon-rich absorbent from the upstream is divided into a third liquid phase stream and a fourth liquid phase stream, the flow ratio of the third liquid phase stream to the fourth liquid phase stream is 1: 9-9: 1, the third liquid phase stream is introduced into the primary flash tank (1), and the fourth liquid phase stream is introduced into the upper part of the lower section of the secondary flash tank (2); dividing a sulfur-rich absorbent from the upstream into a fifth liquid-phase stream and a sixth liquid-phase stream, wherein the flow ratio of the fifth liquid-phase stream to the sixth liquid-phase stream is 1: 50-50: 1, the fifth liquid-phase stream is introduced into the stripping tower (5), the sixth liquid-phase stream is introduced into the upper part of the lower section of the secondary flash tank (2), the stripping nitrogen is divided into a third gas-phase stream and a fourth gas-phase stream, and the flow ratio of the third gas-phase stream to the fourth gas-phase stream is 1: 0-20: 1; the third vapour phase stream is directed to the stripper (5) and the fourth vapour phase stream is directed to the four-stage flash drum (4).
4. A method of regenerating a semi-lean absorbent according to any one of claims 1 to 3, characterized in that: the three-level flash tank (3) and the four-level flash tank (4) share the same tank body, and a flash baffle plate (32) and an overflow baffle plate (42) are arranged in the tank body; the lower end edge of the flash separation plate (32) is suspended, the rest of the periphery is connected with the inner wall of the tank body, the upper end edge of the overflow separation plate (42) is suspended, the rest of the periphery is connected with the inner wall of the tank body, the suspended end of the flash separation plate (32) and the suspended end of the overflow separation plate (42) are partially overlapped in the vertical direction, a gap is reserved between the overlapped parts, the inner cavity of the tank body is divided into a first cavity and a second cavity, the two cavities are communicated through the gap between the flash separation plate (32) and the overflow separation plate (42), the first cavity is the third-level flash tank (3), and the second cavity is the fourth-level flash tank (4).
5. The semi-lean absorbent regeneration method of claim 4, characterized in that: the first-stage flash tank (1), the second-stage flash tank (2), the third-stage flash tank (3), the fourth-stage flash tank (4) and the stripping tower (5) share the same tower body, the tower body is sequentially divided into seven sections from top to bottom, wherein the first section is the first-stage flash tank (1), the second section and the third section are the second-stage flash tank (2), the fourth section is a combined tank body shared by the third-stage flash tank (3) and the fourth-stage flash tank (4), and the V section, the VI section and the VII section are the stripping tower (5); the second-stage flash tank (2) is isolated from the third-stage flash tank by a first liquid collecting tray (21) provided with a gas lifting cap, the fourth stage of the combined tank body is isolated from the V stage of the gas stripping tower (5) by a first seal head (31), the V stage of the gas stripping tower (5) is isolated from the VI stage of the gas stripping tower (5) by a second liquid collecting tray (51) provided with a gas lifting cap, the VI stage of the gas stripping tower (5) is isolated from the VII stage by a third liquid collecting tray (52) provided with a gas lifting cap, the bottom of the V stage of the gas stripping tower (5) is connected with the upper part of the VI stage of the gas stripping tower (5) by a first circulating pump (8), and the bottom of the VI stage of the gas stripping tower (5) is connected with the upper part of the VII stage of the gas stripping tower (5) by a second circulating pump (9).
6. The semi-lean absorbent regeneration method of claim 4, characterized in that: the first-stage flash tank (1), the second-stage flash tank (2) and the stripping tower (5) share the same tower body, and the tower body is sequentially divided into six sections from top to bottom, wherein the first section is the first-stage flash tank (1), the second and third sections are the second-stage flash tanks (2), and the V section, the VI section and the VII section are the stripping tower (5); the second section and the third section of the secondary flash tank (2) are separated by a first liquid collecting tray (21) provided with an air lifting cap, the section III of the secondary flash tank (2) is separated from the section V of the stripping tower (5) by a second seal head (22), the section V and the section VI of the stripper tower (5) are separated by a second liquid collecting tray (51) provided with an air lifting cap, the VI section and the VII section of the stripper tower (5) are separated by a third liquid collecting tray (52) provided with a gas lifting cap, the bottom of the section V of the stripping tower (5) is connected with the upper part of the section VI of the stripping tower (5) through a first circulating pump (8), the bottom of the VI section of the stripping tower (5) is connected with the upper part of the VII section of the stripping tower (5) through a second circulating pump (9), and the combined tank body shared by the three-level flash tank (3) and the four-level flash tank (4) is independently arranged.
7. The semi-lean absorbent regeneration method of claim 4, characterized in that: the gas stripping tower (5) is divided into three sections, namely a V section, a VI section and a VII section, wherein the VI section and the VII section which are arranged up and down share a first tower body, the V section of the gas stripping tower (5) and the first-stage flash tank (1), the second-stage flash tank (2), the third-stage flash tank (3) and the fourth-stage flash tank (4) share a second tower body, the second tower body is sequentially divided into five sections from top to bottom, wherein the first section is the first-stage flash tank (1), the second section and the third section are the second-stage flash tank (2), the second section and the third section of the second-stage flash tank (2) are isolated by a first liquid collecting tray (21) provided with an air lifting cap, and the IV section is a combined tank body shared by the third-stage flash tank (3) and the fourth-stage flash tank (4); the combined tank body is isolated from the section V of the stripping tower (5) through a first seal head (31), a section VI and a section VII of the stripping tower (5) are isolated through a third liquid collecting tray (52) provided with a gas lifting cap, the bottom of the section V of the stripping tower (5) is connected with the upper part of the section VI of the stripping tower (5) through a first circulating pump (8), and the bottom of the section VI of the stripping tower (5) is connected with the upper part of the section VII of the stripping tower (5) through a second circulating pump (9).
8. The semi-lean absorbent regeneration method of claim 4, characterized in that: the gas stripping tower (5) is divided into three sections, namely a V section, a VI section and a VII section, wherein the VI section and the VII section which are arranged up and down share a first tower body, the V section of the gas stripping tower (5) and the first-stage flash tank (1) and the second-stage flash tank (2) share a second tower body, the second tower body is divided into four sections from top to bottom in sequence, wherein the first section is the first-stage flash tank (1), and the second section and the third section are the second-stage flash tank (2); the combined type gas stripping device is characterized in that a first liquid collecting tray (21) provided with a gas lifting cap is adopted between the second section and the third section of the second-stage flash tank (2) to be isolated, the third section of the second-stage flash tank (2) is isolated from the V section of the gas stripping tower (5) through a second seal head (22), the VI section of the gas stripping tower (5) is isolated from the VII section through a third liquid collecting tray (52) provided with the gas lifting cap, the bottom of the V section of the gas stripping tower (5) is connected with the upper portion of the VI section of the gas stripping tower (5) through a first circulating pump (8), the bottom of the VI section of the gas stripping tower (5) is connected with the upper portion of the VII section of the gas stripping tower (5) through a second circulating pump (9), and the combined tank body shared by the third-stage flash tank (3) and the fourth-stage flash tank (4) is independently arranged.
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| JP6088240B2 (en) * | 2012-12-20 | 2017-03-01 | 三菱日立パワーシステムズ株式会社 | Carbon dioxide recovery device and method of operating the recovery device |
| CN107011950B (en) * | 2016-01-28 | 2019-12-27 | 惠生工程（中国）有限公司 | Gas purification method for coal-based natural gas synthesis device |
| CN206276196U (en) * | 2016-06-15 | 2017-06-27 | 中石化宁波工程有限公司 | A kind of CO high2The energy-saving gas cleaning unit of the rate of recovery |
| CN106281476B (en) * | 2016-08-31 | 2019-05-24 | 上海倍能化工技术有限公司 | A kind of method of sour gas in low temperature washing device for methanol and a kind of removing synthesis gas |
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