METHOD AND DEVICE FOR WASHING AND PURIFICATION WITH LOW-TEMPERATURE METHANOL

Abstract

A method for washing and purification with a low-temperature methanol at least includes the following steps: condensing a raw shift gas and conducting a gas-liquid separation to obtain CO.sub.2-containing liquid and a separated raw material gas; and vaporizing the CO.sub.2-containing liquid and reducing a pressure by an expansion to obtain a CO.sub.2-containing gas; and washing the separated raw material gas with a methanol to obtain a purified gas. The present application combines CO.sub.2 condensation and an expander, so that the load of cooling capacity of the system for washing with a low-temperature methanol is reduced by 60%. At the same time, the external work done by the expander reduces the energy consumption of the system. After the CO.sub.2 in the purifying gas of desulfurization in the section A of the scrubber is condensed, the amount of CO.sub.2 entering the section B is reduced.

Claims

1. A method for washing and purification with a low-temperature methanol, comprising: condensing a raw shift gas and conducting a gas-liquid separation to obtain a CO.sub.2-containing liquid and a separated raw material gas; and vaporizing the CO.sub.2-containing liquid and reducing a pressure by an expansion to obtain a CO.sub.2-containing gas; and washing the separated raw material gas with the low-temperature methanol to obtain a purified gas.

2. The method according to claim 1, wherein the vaporizing the CO.sub.2-containing liquid and reducing the pressure by the expansion comprises: a. after the reducing the pressure, flashing the CO.sub.2-containing liquid to obtain an effective gas, wherein the effective gas is compressed and returns to the raw shift gas; b. evaporating a flashed liquid phase to obtain a CO.sub.2-containing medium pressure gas; and c. delivering the CO.sub.2-containing medium pressure gas into an expander and reducing the pressure by the expansion to obtain a low-pressure CO.sub.2-containing gas; before delivering the CO.sub.2-containing medium pressure gas into the expander, the step c further comprises: performing a heat exchange and a heating to the CO.sub.2-containing medium pressure gas.

3. The method according to claim 1, further comprising conducting a desulfurization treatment to the raw shift gas before condensing the raw shift gas and conducting the gas-liquid separation; wherein the desulfurization treatment comprises: cooling and separating the raw shift gas and separating methanol and water in the raw shift gas to obtain a shift gas; delivering the shift gas into a scrubber; and desulfurizing the shift gas with a sulfur-free rich methanol; after the CO.sub.2-containing gas is heat-exchanged, the CO.sub.2-containing gas is mixed with a CO.sub.2 gas obtained from a recovery system as a CO.sub.2 product gas, and the CO.sub.2 product gas is sent out of a boundary area; and or, after the CO.sub.2-containing gas is heated by a heat exchange, the CO.sub.2-containing gas is mixed with the CO.sub.2 gas obtained from the recovery system and heated again as the CO.sub.2 product gas and then is sent out of the boundary area.

4. The method according to claim 1, further comprising: desulfurizing the CO.sub.2-containing gas; the desulfurizing comprising: delivering the CO.sub.2-containing gas into a CO.sub.2 desorption tower of a recovery system for a desulfurization; after a desulfurized CO.sub.2 gas is heat-exchanged, the desulfurized CO.sub.2 gas serves as a CO.sub.2 product gas and then is sent out of a boundary area.

5. A device for washing and purification with a low-temperature methanol, comprising: a heat exchange condensing device, a CO.sub.2 condensate separator, an expander, and a scrubber; wherein a feed port of the CO.sub.2 condensate separator is connected to a raw material gas pipeline, and the heat exchange condensing device is provided on the raw material gas pipeline; a gas outlet of the CO.sub.2 condensate separator is connected to the scrubber through a first pipeline; a liquid outlet of the CO.sub.2 condensate separator is connected to the heat exchange condensing device and the expander sequentially through second pipelines; and a gas outlet of the scrubber is connected to a purified gas pipeline; and the scrubber is used to wash a gas separated by the CO.sub.2 condensate separator.

6. The device according to claim 5, wherein the heat exchange condensing device comprises a purifying gas condenser, a CO.sub.2 condensate evaporator, and a purified gas cryogenic device; the raw material gas pipeline is respectively connected to a heating chamber of the purifying gas condenser and a heating chamber of the CO.sub.2 condensate evaporator; the purifying gas condenser and the feed port of the CO.sub.2 condensate separator are connected through a third pipeline; the heating chamber of the CO.sub.2 condensate evaporator is connected to the feed port of the CO.sub.2 condensate separator through a fourth pipeline, and the purified gas cryogenic device is provided on the fourth pipeline; the liquid outlet of the CO.sub.2 condensate separator is connected to an evaporation chamber of the CO.sub.2 condensate evaporator and an inlet of the expander through fifth pipelines in sequence; and an outlet of the expander is connected to a carbon dioxide product gas pipeline through the purifying gas condenser.

7. The device according to claim 5, wherein the raw material gas pipeline is provided with a shift gas condenser and a shift gas separator in sequence along a direction of a gas flow; the shift gas condenser is used to cool a raw shift gas; the shift gas separator is used to separate methanol and water in a cooled raw shift gas; a gas outlet of the shift gas separator is connected to the scrubber through a third pipeline; or the gas outlet of the shift gas separator is respectively connected to the purifying gas condenser and the CO.sub.2 condensate evaporator through fourth pipelines; a liquid outlet of the shift gas separator is connected to a recovery system through a fifth pipeline; and the shift gas condenser is respectively located on a pipeline between the CO.sub.2 condensate separator and the expander, on a carbon dioxide product gas pipeline, and on the purified gas pipeline.

8. The device according to claim 7, wherein the scrubber comprises a first section and a second section from bottom to top; the first section of the scrubber is used to wash the gas separated by the CO.sub.2 condensate separator; the second section of the scrubber is used to desulfurize the raw shift gas; a lower part of the first section of the scrubber is connected to the gas outlet of the shift gas separator through the third pipeline; an upper part of the first section of the scrubber is respectively connected to a heating chamber of the purifying gas condenser and a heating chamber of the CO.sub.2 condensate evaporator through sixth pipelines; a lower part of the second section of the scrubber is connected to the gas outlet of the CO.sub.2 condensate separator through the first pipeline; and the gas outlet at a top of the second section of the scrubber is connected to the purified gas pipeline.

9. The device according to claim 8, wherein an outlet of the expander is connected to a feed port of a CO.sub.2 desorption tower of the recovery system via the purifying gas condenser through a seventh pipeline; and a discharge port of the CO.sub.2 desorption tower is connected to the carbon dioxide product gas pipeline through the shift gas condenser.

10. The device according to claim 7, further comprising a flash tank, wherein a liquid inlet of the flash tank is connected to the liquid outlet of the CO.sub.2 condensate separator through a sixth pipeline; a gas outlet of the flash tank is connected to the raw material gas pipeline; a liquid outlet of the flash tank is connected to an evaporation chamber of the CO.sub.2 condensate evaporator through a seventh pipeline; and a compressor is provided on a pipeline connecting the flash tank and the raw material gas pipeline.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0065] FIG. 1 is the structure and process schematic diagram of the device for washing and purification with a low-temperature methanol in one embodiment of the present application.

[0066] FIG. 2 is the structure and process schematic diagram of the device for washing and purification with a low-temperature methanol in the other embodiment of the present application.

REFERENCE NUMERALS

[0067] T-101: scrubber; E-101: shift gas condenser; E-102: purifying gas condenser; E-103: CO.sub.2 condensate evaporator; E-104: purified gas cryogenic device; V-101: shift gas separator; V-102: CO.sub.2 condensate separator; V-103: flash tank; G-101: expander; and K-101; compressor.

[0068] 1: shift gas; 2: tail gas; 3: CO.sub.2 product gas; 4; purified gas; 5: separated shift gas; 6: methanol and water; 7: desulfurized purified gas; 7-1: sulfur-containing CO.sub.2 gas; 8: sulfur-containing rich methanol; 9: sulfur-free rich methanol for reflux; 10: sulfur-free rich methanol; 11: CO.sub.2 condensate; 12: purified gas after liquid separation; 13: medium-pressure CO.sub.2 gas; 14: condensate after flash; 15: circulated gas; 16: lean methanol; and 17: spray lean methanol.

DETAILED DESCRIPTION OF THE EMBODIMENTS

[0069] The present disclosure will be described in detail below in conjunction with the drawings and embodiments, but the present application is not limited to these embodiments.

[0070] One embodiment of the present application provides a device for washing and purification with a low-temperature methanol. The structure of the device is shown in FIG. 1. The device includes a scrubber T-101, a heat exchange condensing device, a CO.sub.2 condensate separator V-102, and an expander G-101.

[0071] A raw material gas pipeline is connected to a feed port of the CO.sub.2 condensate separator V-102 through a pipeline, and the heat exchange condensing device is provided on the pipeline.

[0072] A gas outlet of the CO.sub.2 condensate separator V-102 is connected to a lower part of the scrubber T-101 through a pipeline. A liquid outlet of the CO.sub.2 condensate separator V-102 is connected to the heat exchange condensing device and the expander G-101 in sequence through pipelines.

[0073] A top of the scrubber T-101 is connected to the purified gas pipeline.

[0074] The heat exchange condensing device includes a purifying gas condenser E-102, a CO.sub.2 condensate evaporator E-103, and a purified gas cryogenic device E-104.

[0075] The raw material gas pipeline is respectively connected to the heating chambers of the purified gas cryogenic device E-102 and the CO.sub.2 condensate evaporator E-103.

[0076] The purified gas cryogenic device E-102 and the feed port of the CO.sub.2 condensate separator V-102 are connected through a pipeline.

[0077] The heating chamber of the CO.sub.2 condensate evaporator E-103 is connected to the feed port of the CO.sub.2 condensate separator V-102 through a pipeline, and the purified gas cryogenic device E-104 is provided on the pipeline.

[0078] The liquid outlet of the CO.sub.2 condensate separator V-102 is connected to an evaporation chamber of the CO.sub.2 condensate evaporator E-103 and an inlet of the expander G-101 through pipelines in sequence.

[0079] The outlet of the expander G-101 is connected to a carbon dioxide product gas pipeline through the purifying gas condenser E-102. Or as another embodiment of the present application shown in FIG. 2, the outlet of the expander G-101 is connected to the carbon dioxide product gas pipeline through the purifying gas condenser E-102 and the recovery system sequentially.

[0080] The raw material gas pipeline is provided with a shift gas condenser E-101 and a shift gas separator V-101 in sequence along a direction of a gas flow.

[0081] The shift gas condenser E-101 is used to cool the raw shift gas.

[0082] The shift gas separator V-101 is used to separate methanol and water in the cooled raw shift gas.

[0083] The gas outlet of the shift gas separator V-101 is connected to the scrubber T-101 through a pipeline. Or as another embodiment of the present application shown in FIG. 2, the gas outlet of the shift gas separator is respectively connected to the purifying gas condenser and the CO.sub.2 condensate evaporator through pipelines.

[0084] The liquid outlet of the shift gas separator V-101 is connected to the methanol recovery system through a pipeline.

[0085] The shift gas condenser E-101 is respectively located on the pipeline between the CO.sub.2 condensate separator V-102 and the expander, on the carbon dioxide product gas pipeline, and on the purified gas pipeline.

[0086] The shift gas condenser E-101 is also located on the tail gas pipeline.

[0087] In an embodiment of the present application, as shown in FIG. 1, the scrubber T-101 includes a section A and a section B from bottom to top.

[0088] The section A of the scrubber T-101 is used to wash the gas separated by the CO.sub.2 condensate separator V-102.

[0089] The section B of the scrubber T-101 is used to desulfurize the raw shift gas.

[0090] A lower part of the section A of the scrubber T-101 is connected to the gas outlet of the shift gas separator V-101 through a pipeline.

[0091] An upper part of the section A of the scrubber T-101 is connected to the heating chamber of the purifying gas condenser E-102 and the heating chamber of the CO.sub.2 condensate evaporator E-103 through pipelines.

[0092] A lower part of the section B of the scrubber T-101 is connected to the gas outlet of the CO.sub.2 condensate separator V-102 through a pipeline.

[0093] The gas outlet at a top of the section B of the scrubber is connected to the purified gas pipeline.

[0094] The device also includes a flash tank V-103.

[0095] The liquid inlet of the flash tank V-103 is connected to the liquid outlet of the CO.sub.2 condensate separator V-102 through a pipeline.

[0096] The gas outlet of the flash tank V-103 is connected to the raw material gas pipeline.

[0097] The liquid outlet of the flash tank V-103 is connected to the evaporation chamber of the CO.sub.2 condensate evaporator E-103 through a pipeline.

[0098] A compressor K-101 is provided on the pipeline connecting the flash tank V-103 and the raw material gas pipeline.

[0099] According to one embodiment of the present disclosure shown in FIG. 1, a method for washing and purification with a low-temperature methanol is as follows:

[0100] The raw shift gas for washing with a low-temperature methanol is cooled by the shift gas condenser E-101. The shift gas separator V-101 separates methanol and water to obtain the shift gas. After the methanol and water of the shift gas were separated by the shift gas separator V-101, the shift gas enters the section A of the scrubber T-101 and is desulfurized with some sulfur-free rich methanol. The sulfur-free raw material gas is guided out of the section A of the scrubber T-101 and then is cooled by the purifying gas condenser E-102, the CO.sub.2 condensate evaporator E-103, and the heat exchanger E-104, where some CO.sub.2 is condensed and enters the CO.sub.2 condensate separator V-102 for separation. The gas obtained from the CO.sub.2 condensate separator V-102 enters the section B of the scrubber T-101 and is washed with lean methanol until the CO.sub.2 meets the requirements for the downstream process. Subsequently, the gas exchanges heat through the purifying gas condenser E-102 and the shift gas condenser E-101 and then was guided out of the boundary area. The high-pressure liquid CO.sub.2 separated by the CO.sub.2 condensate separator V-102 is decompressed and then flashed in the flash tank V-103 to obtain useful gas, which is compressed by the circulation gas compressor K-101 together with the medium-pressure flash gas and then returned to the raw material gas. The medium-pressure CO.sub.2 liquid obtained from the flash tank V-103 is heat-exchanged and vaporized in the CO.sub.2 condensate evaporator E-103, and the cooling capacity is recovered from the raw shift gas. The vaporized medium-pressure CO.sub.2 gas is reheated by the shift gas condenser E-101 and then enters the expander G-101. The expander G-101 does external work to obtain the low-temperature and low-pressure CO.sub.2 gas, which exchanges heat by the purifying gas condenser E-102 and then is combined with the CO.sub.2 product gas of the system. After being exchanged heat by the shift gas condenser E-101, it is delivered out of the boundary area.

[0101] According to another embodiment of the present disclosure, a method for washing and purification with a low-temperature methanol is as follows:

[0102] The raw shift gas for washing with a low-temperature methanol is cooled by the shift gas condenser E-101. The shift gas separator V-101 separates methanol and water to obtain the shift gas. After the shift gas is cooled by the purifying gas condenser E-102, the CO.sub.2 condensate evaporator E-103, and the heat exchanger E-104, some CO.sub.2 is condensed and enters the CO.sub.2 condensate separator V-102 for separation. The gas obtained from the CO.sub.2 condensate separator V-102 enters the lower part of the section A of the scrubber T-101 for desulfurization. At this time, the section A and the section B of the scrubber T-101 are no longer separated, and the gas in the section A enters the section B through a chimney. The top of the scrubber T-101 is washed with lean methanol until the CO.sub.2 meets the requirements for the downstream process. Subsequently, the gas exchanges heat through the purifying gas condenser E-102 and the shift gas condenser E-101 and then was guided out of the boundary area. The high-pressure liquid CO.sub.2 separated by the CO.sub.2 condensate separator V-102 is decompressed and then flashed in the flash tank V-103 to obtain useful gas, which is compressed by the circulation gas compressor K-101 together with the medium-pressure flash gas and then returned to the raw shift gas. The medium-pressure CO.sub.2 liquid obtained from the flash tank V-103 is heat-exchanged and vaporized in the CO.sub.2 condensate evaporator E-103, and the cooling capacity is recovered from the raw shift gas. The vaporized medium-pressure CO.sub.2 gas is reheated by the shift gas condenser E-101 and then enters the expander G-101. The expander G-101 does external work to obtain the low-temperature and low-pressure sulfur-containing CO.sub.2 gas (7-1), which exchanges heat by the purifying gas condenser E-102 and then enters the CO.sub.2 desorption tower of the methanol recovery system for desulfurization. The obtained desulfurized CO.sub.2 gas exchanges heat through the shift gas condenser E-101 and then is delivered to the boundary area as CO.sub.2 product gas.

Example 1

[0103] A pressure 5.7 MPaG of a raw shift gas (1) including H.sub.2 53.60%, CO.sub.2 44.76%, H.sub.2S 0.15%, CO 0.97%, saturated water, and other components is mixed with a circulation gas (15) and spray lean methanol (17) and then enters the shift gas condenser E-101 to be cooled to ?14? C. After methanol and water (6) are separated by the shift gas separator V-101, the separated shift gas (5) enters the section A of the scrubber T-101 to be desulfurized with sulfur-free rich methanol (9) for reflux. The sulfur content of the desulfurized purified gas (7) is less than 1 ppm. The desulfurized purified gas is guided out of the upper part of the section A of the scrubber T-101 and then is cooled to ?32? C. via a heat change at the purifying gas condenser E-102, the CO.sub.2 condensate evaporator E-103, and the purified gas cryogenic device E-104. After cooling down, a large amount of CO.sub.2 in the desulfurized purified gas is condensed into the liquid, which is separated in the CO.sub.2 condensate separator V-102. The purified gas (12) after the liquid separation returns to the section B of the scrubber T-101 to be washed with methanol until the CO.sub.2 meets the purification requirements, thereby obtaining a purified gas (4).

[0104] The high-concentration CO.sub.2 condensate (11) separated by the CO.sub.2 condensate separator V-102 is flashed to obtain an effective gas such as H.sub.2 in the flash tank V-103 after the pressure is reduced. The flash gas enters the circulation gas compressor K-101 to be compressed and then returns to the raw shift gas (1). The liquid phase in the flash tank V-103 (14) enters the CO.sub.2 condensate evaporator E-103. The liquid CO.sub.2 evaporates in the CO.sub.2 condensate evaporator E-103 and provides cooling capacity for desulfurized purified gas. After evaporation, the obtained medium-pressure CO.sub.2 gas (13) with a pressure of about 1.9 MPa exchanges heat via the shift gas condenser E-101 until reaching 30? C. before entering the expander G-101. The temperature of the CO.sub.2 gas decreases by reducing the pressure with expansion and does external work to obtain a low-temperature CO.sub.2 gas with a pressure of 0.38 MPaA and a temperature of ?67? C. After heat exchanging with the purifying gas condenser of desulfurization E-102, the low-temperature CO.sub.2 gas is mixed with the CO.sub.2 gas obtained by a low-pressure flashing from the recovery system and re-heats to 30? C. by the shift gas condenser E-101 as a CO.sub.2 product gas (3). The CO.sub.2 product gas is then delivered out of the boundary area.

[0105] The methanol and water separated by the shift gas separator V-101, sulfur-containing rich methanol (8) obtained from the scrubber T-101, and sulfur-free rich methanol (10) are delivered to the methanol recovery system for recovery. The tail gas (2) of the system is discharged after heat exchanging with the purifying gas condenser of desulfurization E-102 and the shift gas condenser E-101.

Example 2

[0106] The conditions are the same as those in Example 1 except that the pressure is not reduced through an expansion after CO.sub.2 is condensed.

Example 3

[0107] Comparing the energy consumption of the method of washing with a low-temperature methanol of Example 1 and that of Example 2, the results are as follows:

TABLE-US-00001 Process in Example 2 Process in Example 1 Conditions flow: 288579 Nm.sup.3/h flow: 288579 Nm.sup.3/h of raw temperature: 40? C. temperature: 40? C. shift gas pressure: 5.7 MPaG pressure: 5.7 MPaG content of CO.sub.2: 44.76% mol content of CO.sub.2: 44.76% mol Indicators cooling capacity consumption cooling capacity consumption of main (?38? C.): 4450 kW (?38? C.): 1715 kW con- steam: 13.8 t/h steam: 12.8 t/h sumption nitrogen stripping: 12000 nitrogen stripping: 9800 Nm.sup.3/h Nm.sup.3/h Scrubber 3800 mm 3000 mm diameter

[0108] It can be seen from the above table that by combining the CO.sub.2 condensation with the expander, the cooling capacity consumption of the process of washing with the low-temperature methanol is greatly reduced. The consumption of steam and the consumption of nitrogen stripping used in the process are also significantly reduced. At the same time, the diameter of the scrubber used to wash is also significantly reduced, which greatly reduces the production cost of the process of washing with a low-temperature methanol.

[0109] The above examples are only several embodiments of the present application and do not limit the present application in any form. Although the present application discloses several preferred embodiments as shown above, these embodiments do not used to limit the present application. Any professional familiar with the technique can make changes or modifications based on the above disclosure without departing from the scope of the technical solution of the present application, and these changes or modifications equal to equivalent embodiments and all belong to the scope of the technical solution.