CN116099332A - Improved method of methanol scrubbing and stripping process - Google Patents
Improved method of methanol scrubbing and stripping process Download PDFInfo
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- CN116099332A CN116099332A CN202310108784.9A CN202310108784A CN116099332A CN 116099332 A CN116099332 A CN 116099332A CN 202310108784 A CN202310108784 A CN 202310108784A CN 116099332 A CN116099332 A CN 116099332A
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- gas
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- carbon dioxide
- stripping
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 87
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000005201 scrubbing Methods 0.000 title claims abstract description 6
- 239000007789 gas Substances 0.000 claims abstract description 163
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 138
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 69
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 69
- 238000000926 separation method Methods 0.000 claims abstract description 36
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 32
- 238000001179 sorption measurement Methods 0.000 claims abstract description 32
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 16
- 238000005262 decarbonization Methods 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 12
- 239000002699 waste material Substances 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract 1
- 229910001882 dioxygen Inorganic materials 0.000 abstract 1
- 238000005261 decarburization Methods 0.000 description 10
- 238000007701 flash-distillation Methods 0.000 description 10
- 238000011084 recovery Methods 0.000 description 7
- 238000005406 washing Methods 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 230000006837 decompression Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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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
-
- 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
- B01D53/1412—Controlling the absorption process
-
- 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
- B01D53/1475—Removing carbon dioxide
-
- 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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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses an improved method of a methanol scrubbing and stripping process, which is characterized in that two or more stripping towers or 2 or more gas inlets are arranged in the same stripping tower; one of the first-stage inlet gas of the stripping tower is the outlet gas of the first-stage adsorption separation device of liquefied non-condensable gas, wherein the concentration of carbon dioxide is 3-10%, and the other is the second-stage stripping gas of the stripping tower, and the concentration of carbon dioxide is more than 10%; the gas at the last stage of the gas stripping tower adopts the outlet gas of an adsorption separation device, wherein the concentration of carbon dioxide is below 10 ppm; the concentration of carbon dioxide in the gas at the outlet of the stripping tower is 70-83%, the carbon dioxide is compressed and adsorbed and separated to 3-10% to form first-stage decarbonizing gas, one part of the first-stage decarbonizing gas is used as the first-stage inlet gas of the stripping tower, the other part of the first-stage decarbonizing gas is sent to the adsorption and separation system of the last stage, and the gas with the carbon dioxide concentration less than 10ppm at the outlet is obtained and is called the last-stage decarbonizing gas, and the last-stage inlet gas of the stripping tower is sent. Thus, the stripping amount of pure nitrogen in the traditional process can be reduced or stopped by obtaining high-concentration dioxygen.
Description
Technical Field
The invention relates to the fields of chemical industry, environmental protection and energy conservation, and discloses an improved method for a methanol scrubbing and stripping process.
Background
The methanol washing process is to useMethanol at low temperature to CO 2 And (3) carrying out physical absorption on the acid gas, and selectively removing the acid gas in the raw material gas to obtain a purified gas product. CO absorption 2 The methanol rich liquid is usually regenerated by nitrogen stripping, a large amount of pure nitrogen is consumed, and the stripped CO-containing liquid contains 2 The tail gas is difficult to be utilized and directly discharged.
CN202110882632.5 discloses a high-efficient composite low-temperature methanol-washing CO 2 Recovery tower is directed at rich methanol solution CO in acid gas low temperature methanol washing technology 2 、H 2 S separation, inventing a high-efficiency composite low-temperature methanol washing CO 2 The recovery tower is used for eliminating nitrogen stripping; the invention has two schemes: for a newly built device, the methanol-rich liquid CO 2 Separation of the crude H used 2 S concentration tower and nitrogen stripping tower, most of cold and heat exchange recovery process are integrated in one tower; old device is modified: the original methanol-rich liquid CO 2 The nitrogen stripping tower used for separation and a part of cold and heat exchange recovery process are integrated in one tower with high efficiency.
CN202221269266.2 discloses a device for reducing the emission of effective gas in a low-temperature methanol washing and purifying process, wherein a methanol-rich pipeline is connected with a methanol-rich stripping tower; the top of the methanol-rich stripping tower is connected with a condensing heat exchanger; the bottom of the methanol-rich stripping tower is connected with an evaporation heat exchanger; the condensing heat exchanger is connected with the separating tank; the bottom of the separating tank is connected with the evaporating heat exchanger; the evaporative heat exchanger is connected to the methanol rich line. And a methanol-rich decompression control valve is arranged on the connecting pipeline of the methanol-rich pipeline and the methanol-rich stripping tower. The top of the separating tank is connected with a pipeline of the circulating gas through a pressure control valve. The flash evaporation gas rich in methanol is condensed to obtain liquid carbon dioxide, the liquid carbon dioxide is heated and gasified to serve as a gas stripping gas source rich in methanol, the condensed flash evaporation gas is recycled, the content of effective gas in the rich methanol is greatly reduced, the effective gas loss in the gas purification process is reduced, and the environment pollution of energy conservation, consumption reduction and gas emission is reduced.
CN202220222012.9 discloses a device for recovering energy of low-temperature methanol washing tail gas by fractional gas stripping, which comprises a sulfur-free flash distillation tower, a sulfur-containing flash distillation tower and a gas stripping tower, wherein the top of the sulfur-free flash distillation tower is sequentially connected with a first pressure reducing valve and sulfur-free methanol pipelines from medium pressure flash distillation through pipelines, the bottom of the sulfur-free flash distillation tower is sequentially connected with a second pressure reducing valve, the top of the sulfur-free flash distillation tower, a fifth pressure reducing valve and the top of the hydrogen sulfide concentration tower through pipelines, the top of the sulfur-containing flash distillation tower is sequentially connected with a third pressure reducing valve and sulfur-containing methanol pipelines from medium pressure flash distillation through pipelines, and the bottom of the sulfur-containing flash distillation tower is sequentially connected with a fourth pressure reducing valve, the top of the sulfur-containing flash distillation tower, a sixth pressure reducing valve and a middle feed inlet of the hydrogen sulfide concentration tower.
Although the process of the methanol gas washing increases effective gas and CO 2 Etc. recovery or cold recovery, but the recovery mode often requires a large amount of separation energy consumption, and is not economical.
Disclosure of Invention
Aiming at the problems, the invention provides an improved method of a methanol scrubbing and stripping process, which is characterized in that: two or more gas stripping towers are arranged, or 2 or more gas inlets are designed in the same gas stripping tower; one of the first-stage inlet gas of the stripping tower is the outlet gas of the first-stage adsorption separation device of liquefied non-condensable gas, wherein the concentration of carbon dioxide is 3-10%, and the other is the second-stage stripping gas of the stripping tower, and the concentration of carbon dioxide is more than 10%; the gas at the last stage of the gas stripping tower adopts the outlet gas of the last stage of the adsorption separation device, wherein the concentration of carbon dioxide is below 10 ppm; the concentration of carbon dioxide in the gas at the outlet of the stripping tower is 70-83%, the process of compressing, adsorbing and separating the carbon dioxide to 3-10% is called primary decarburization gas, one part of the primary decarburization gas is used as the inlet gas of the first stage of the stripping tower, the other part of the primary decarburization gas is sent to the adsorption and separation system of the last stage, and the gas with the carbon dioxide concentration of less than 10ppm at the outlet is called the final stage decarburization gas, and the final stage inlet gas of the stripping tower is sent. Thereby reducing or disabling the energy waste of the conventional process stripper using pure nitrogen as stripping inlet gas while obtaining high concentration carbon dioxide or liquid carbon dioxide.
Preferably, the two or more stripping towers are two, and the 2 or more gas inlets are 2.
The process when the same stripping column is designed with 3 gas inlets is as follows: one of the first-stage inlet gas of the stripping tower is the outlet gas of the first-stage adsorption separation device of liquefied non-condensable gas, wherein the concentration of carbon dioxide is 3-10%, and the other is the second-stage stripping gas of the stripping tower, and the concentration of carbon dioxide is more than 10%; one of the second-stage inlet gas of the stripping tower is the outlet gas of the second-stage adsorption separation device, wherein the concentration of carbon dioxide is 1-3%, the other is the third-stage stripping gas of the stripping tower, and the concentration of carbon dioxide is more than 3%; the third stage inlet gas of the stripping tower adopts the outlet gas of a third stage adsorption separation device, wherein the concentration of carbon dioxide is below 10 ppm; the concentration of carbon dioxide in the gas at the outlet of the stripping tower is 70-83%, the compression and adsorption separation of carbon dioxide to 3-10% are called primary decarburization gas, one part is used as the gas at the inlet of the first stage of the stripping tower, and the other part is continuously sent to the second stage for adsorption separation of carbon dioxide to 1-3% are called secondary decarburization gas; the second-stage decarbonization gas is partially used as the second-stage inlet gas of the stripping tower, and a part of the second-stage decarbonization gas is sent to a third-stage adsorption separation system, so that gas with the outlet carbon dioxide of less than 10ppm is called third-stage decarbonization gas and is used as the third-stage inlet gas of the stripping tower, thereby reducing or stopping the energy waste of using pure nitrogen as the stripping inlet gas in the conventional process stripping tower while obtaining high-concentration carbon dioxide or liquid carbon dioxide.
The invention has the advantages that:
1. when starting, nitrogen is used as the inlet gas of the stripping tower, and once the circulation starts, no nitrogen is used, or only a small amount of nitrogen is needed to be supplemented, so that the nitrogen is saved;
2. the multistage fractional stripping can use part of low-concentration carbon dioxide gas as stripping inlet gas, can reduce the operation cost of first-stage or first-stage carbon dioxide purification, and simultaneously saves purification investment.
Drawings
FIG. 1 shows the same process flow of 2 gas inlets of a stripping tower.
FIG. 2 shows a series process flow of three-stage stripping towers of the invention.
Description of the embodiments
Other advantages and effects of the present invention will become apparent to those skilled in the art from the following disclosure, which describes the embodiments of the present invention with reference to specific examples. The invention may be practiced or carried out in other embodiments that depart from the specific details, and the details of the present description may be modified or varied from the spirit and scope of the present invention. It should be noted that the following embodiments and features in the embodiments may be combined with each other without conflict.
Example 1: as shown in fig. 1, the same stripping tower is provided with a 2-stage gas inlet, one of the first-stage inlet gas of the stripping tower is the outlet gas of the first-stage adsorption separation device of liquefied non-condensable gas, wherein the concentration of carbon dioxide is 4 percent, and the other is the second-stage stripping gas of the stripping tower, and the concentration of carbon dioxide is 12 percent; the second-stage inlet gas of the stripping tower adopts the outlet gas of a second-stage adsorption separation device, wherein the concentration of carbon dioxide is 8ppm; the concentration of carbon dioxide in the outlet gas of the stripping tower is 80%, the compression and adsorption separation of carbon dioxide to 4% are called primary decarbonization gas, a part of the carbon dioxide is used as primary inlet gas of the stripping tower, a part of the carbon dioxide is sent to a secondary adsorption separation system, 8ppm of outlet carbon dioxide is obtained and is called secondary decarbonization gas, and the secondary inlet gas of the stripping tower is sent to the stripping tower, so that the energy waste of using pure nitrogen as the stripping inlet gas in the traditional process can be reduced or stopped while high-concentration carbon dioxide or liquid carbon dioxide is obtained.
Example 2: the same gas stripping tower is provided with a 3-stage gas inlet, wherein one of the first-stage inlet gas of the gas stripping tower is the outlet gas of a first-stage adsorption separation device of liquefied non-condensable gas, the concentration of carbon dioxide is 5 percent, and the other gas is the gas stripping gas of the second stage of the gas stripping tower, and the concentration of carbon dioxide is 18 percent; the concentration of carbon dioxide in the outlet gas of the second-stage adsorption separation device of the second-stage inlet gas of the stripping tower is 1%, the second-stage inlet gas of the stripping tower is the stripping gas of the third stage of the stripping tower, and the concentration of carbon dioxide in the outlet gas is more than 3%; the third stage inlet gas of the stripping tower adopts the outlet gas of a third stage adsorption separation device, wherein the concentration of carbon dioxide is 5ppm; the concentration of carbon dioxide in the gas at the outlet of the stripping tower is 83%, the compression and adsorption separation of carbon dioxide to 5% are called primary decarburization gas, one part is used as the gas at the inlet of the first stage of the stripping tower, and the other part is continuously sent to the second stage for adsorption separation of carbon dioxide to 1% are called secondary decarburization gas; the second-stage decarbonization gas is partially used as the second-stage inlet gas of the stripping tower, and a part of the second-stage decarbonization gas is sent to a third-stage adsorption separation system, so that 5ppm of gas of outlet carbon dioxide is obtained and is called three-stage decarbonization gas and is used as the third-stage inlet gas of the stripping tower, thereby reducing or stopping the energy waste of using pure nitrogen as the stripping inlet gas in the conventional process while obtaining high-concentration carbon dioxide or liquid carbon dioxide.
Example 3: as shown in fig. 2, three stages of stripping towers are arranged in series, wherein one of the inlet gases of the first stage stripping tower is the outlet gas of the first stage adsorption separation device of liquefied non-condensable gas, the concentration of carbon dioxide is 8 percent, and the other is the stripping gas of the second stage stripping tower, and the concentration of carbon dioxide is 15 percent; one of the inlet gases of the second-stage stripping tower is the outlet gas of the second-stage adsorption separation device, wherein the concentration of carbon dioxide is 1.5 percent, the other is the stripping gas of the third-stage stripping tower, and the concentration of carbon dioxide is 4 percent; the inlet gas of the third-stage stripping tower adopts the outlet gas of the third-stage adsorption separation device, wherein the concentration of carbon dioxide is 6ppm; the concentration of carbon dioxide in the gas at the outlet of the stripping tower is 82%, the compression and adsorption separation of carbon dioxide to 8% are called primary decarburization gas, one part is used as the gas at the inlet of the first-stage stripping tower, and the other part is continuously sent to the second-stage adsorption separation of carbon dioxide to 1.5% are called secondary decarburization gas; the second-stage decarbonization gas is partially used as the inlet gas of the second-stage stripping tower, and a part of the second-stage decarbonization gas is sent to a third-stage adsorption separation system, so that 6ppm of gas of outlet carbon dioxide is obtained and is called three-stage decarbonization gas and is used as the inlet gas of the third-stage stripping tower, thereby reducing or stopping the energy waste of using pure nitrogen as the stripping inlet gas in the traditional process stripping tower while obtaining high-concentration carbon dioxide or liquid carbon dioxide.
Claims (4)
1. An improved method of methanol scrubbing and stripping process is characterized in that 2 or more gas inlets are arranged in the same stripping tower; one of the first-stage inlet gas of the stripping tower is the outlet gas of the first-stage adsorption separation device of liquefied non-condensable gas, wherein the concentration of carbon dioxide is 3-10%, and the other is the second-stage stripping gas of the stripping tower, and the concentration of carbon dioxide is more than 10%; the gas at the last stage of the gas stripping tower adopts the outlet gas of the last stage of the adsorption separation device, wherein the concentration of carbon dioxide is below 10 ppm; the concentration of carbon dioxide in the gas at the outlet of the stripping tower is 70-83%, the compression and adsorption separation of carbon dioxide to 3-10% are called primary decarbonization gas, a part of the primary decarbonization gas is used as the first stage inlet gas of the stripping tower, a part of the primary decarbonization gas is sent to the final stage adsorption separation system, the gas with the concentration of less than 10ppm of the outlet carbon dioxide is obtained and is called final stage decarbonization gas, and the final stage inlet gas of the stripping tower is sent to the stripping tower, so that the energy waste of using pure nitrogen as the stripping inlet gas in the traditional process can be reduced or stopped while high-concentration carbon dioxide or liquid carbon dioxide is obtained.
2. The design of 2 or more gas inlets to the same stripper as defined in claim 1 can be equivalently changed to two or more strippers, each with additional gas inlets.
3. 2 or more gas inlets as claimed in claim 1, preferably 2.
4. Two or more stripper columns according to claim 2, preferably two.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310108784.9A CN116099332A (en) | 2023-02-14 | 2023-02-14 | Improved method of methanol scrubbing and stripping process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310108784.9A CN116099332A (en) | 2023-02-14 | 2023-02-14 | Improved method of methanol scrubbing and stripping process |
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| Publication Number | Publication Date |
|---|---|
| CN116099332A true CN116099332A (en) | 2023-05-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310108784.9A Pending CN116099332A (en) | 2023-02-14 | 2023-02-14 | Improved method of methanol scrubbing and stripping process |
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| Country | Link |
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| CN (1) | CN116099332A (en) |
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2023
- 2023-02-14 CN CN202310108784.9A patent/CN116099332A/en active Pending
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