CN111420515A - Improved low temperature methanol scrubbing of CO2Product gas stripping and pressing process - Google Patents
Improved low temperature methanol scrubbing of CO2Product gas stripping and pressing process Download PDFInfo
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- CN111420515A CN111420515A CN202010153828.6A CN202010153828A CN111420515A CN 111420515 A CN111420515 A CN 111420515A CN 202010153828 A CN202010153828 A CN 202010153828A CN 111420515 A CN111420515 A CN 111420515A
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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
- B01D53/1418—Recovery of products
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
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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
- B01D53/1475—Removing carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
- C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
- C07C273/04—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides an improved low-temperature methanol CO washing method2The product gas stripping and pressing process comprises the following steps: washing low-temperature methanol to absorb CO2Feeding the sulfur-free methanol into a sulfur-free methanol flash tank for flash evaporation; reducing the pressure of the flash evaporated sulfur-free methanol by using a first pressure reducing valve; feeding the decompressed sulfur-free methanol into CO2Flash evaporation is carried out by a flash tank; flashing off CO2The product gas is sent to CO after heat exchange2Compressor inlet, using CO2Compressor pair CO2Pressurizing the product gas, and adding CO after pressurization2The product gas is sent into a urea synthesis tower to synthesize urea; reducing the pressure of the flash evaporated sulfur-free methanol solution by using a second pressure reducing valve, and then sending the reduced sulfur-free methanol solution to a reactorInto CO2Desorbing by using an desorption tower. The process provided by the invention effectively improves the CO at the inlet of the compressor2The air pressure increases the air pumping quantity of the compressor, reduces the power consumption of the compressor and reduces the cost of urea.
Description
Technical Field
The invention relates to the technical field of low-temperature methanol washing, in particular to improved low-temperature methanol washing CO2And (5) a product gas stripping and pressing process.
Background
Low temperature methanol washing is a gas purification process developed jointly by linde corporation and lurgi corporation in germany in the early 50 s of the 20 th century. The first low temperature methanol wash plant was built by lurgi in 1954 in a synthetic fuel plant in south africa. The low-temperature methanol washing process is generally applied to chemical production devices at present. Low temperature methanol scrubbing of CO has long been practiced2The outlet pressure of the product gas is 0.25MPaA, and the product gas is sent to a urea section CO2The inlet of the compressor is pressurized by the compressor and then is used as a urea synthesis raw material, and CO at the inlet of the compressor is frequently generated2Insufficient pressure, insufficient pumping capacity of the compressor, increased power consumption of the compressor, and increased urea cost.
Disclosure of Invention
In view of the above, the present invention provides an improved low temperature methanol CO wash2The invention provides a product gas stripping pressure process which effectively improves the CO at the inlet of a compressor2The air pressure increases the air pumping quantity of the compressor, reduces the power consumption of the compressor and reduces the cost of urea.
The invention provides an improved low-temperature methanol CO washing method2The product gas stripping and pressing process comprises the following steps:
step S1, washing low-temperature methanol to absorb CO2Feeding the sulfur-free methanol into a sulfur-free methanol flash tank for flash evaporation;
step S2, decompressing the sulfur-free methanol flashed in the step S1 by using a first decompression valve;
step S3, sending the sulfur-free methanol decompressed in step S2 to CO2Flash evaporation is carried out by a flash tank;
step S4, the CO flashed off in the step S32The product gas is sent to CO after heat exchange2Compressor inlet, using CO2Compressor pair CO2Pressurizing the product gas, and adding CO after pressurization2The product gas is sent into a urea synthesis tower to synthesize urea; reducing the pressure of the sulfur-free methanol solution flashed in the step S3 by using a second pressure reducing valve, and then sending the reduced pressure sulfur-free methanol solution to CO2Desorbing by using an desorption tower.
Further, in step S1, after the sulfur-free methanol flash drum flash evaporation, the pressure of the sulfur-free methanol was 1.85 MPaA.
Further, in step S2, after the pressure reduction by the first pressure reducing valve, the pressure of the sulfur-free methanol was 0.60 MPaA.
Further, in step S3, the CO is passed2After flash evaporation of the flash tank, CO flashed off2The pressure of the product gas was 0.55 MPaA.
Further, in step S4, the CO is passed2After the compressor is pressurized, CO2The pressure of the product gas was 20 MPaA.
Further, in step S4, after the pressure reduction by the second pressure reducing valve, the pressure of the sulfur-free methanol solution was 0.32 MPaA.
The technical scheme provided by the invention has the beneficial effects that: the process provided by the invention comprises the steps of adding a pressure reducing valve and a low-pressure flash tank after low-temperature methanol washing sulfur-free methanol medium-pressure flash evaporation, and washing CO with low-temperature methanol2The product gas pressure was increased from 0.25MPaA to 0.55 MPaA; CO 22After the pressure of the product gas is increased, the product gas is sent to a urea production device CO2The power consumption of the urea per ton is reduced by about 20 degrees by the inlet of the compressor and the 40 ten thousand ton annual urea production device, the annual effect can reach 470.4 ten thousand yuan, the cost of the urea per ton is effectively saved, and the device has the characteristics of safety, reliability, convenient modification and remarkable economic benefit.
Drawings
FIG. 1 is an improved low temperature methanol CO wash of the present invention2The device schematic diagram of the product gas pressure-stripping process.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, embodiments of the present invention will be further described with reference to the accompanying drawings.
Referring to FIG. 1, an embodiment of the present invention provides an improved low temperature methanol CO wash2The product gas stripping and pressing process comprises the following steps:
washing low-temperature methanol to absorb CO2Feeding the sulfur-free methanol into a sulfur-free methanol flash tank for medium-pressure flash evaporation; reducing the pressure of the sulfur-free methanol subjected to medium-pressure flash evaporation by using a first pressure reducing valve; then the decompressed sulfur-free methanol is sent into CO2Flash evaporation of flash drum, firstly flash to remove CO2Product gas, CO flashed off2The product gas is subjected to heat exchange to obtain CO after heat exchange2The product gas is sent into a urea production device CO2Compressor inlet, using CO2Compressor for mixing CO2The product gas is pressurized step by step, and then the pressurized CO is2The product gas is sent into a urea synthesis tower to synthesize urea; CO is discharged by a second pressure reducing valve2Decompressing the sulfur-free methanol solution flashed by the flash tank, and then feeding the decompressed sulfur-free methanol solution into CO2Desorbing by using an desorption tower.
In FIG. 1, 1 denotes a sulfur-free methanol flash tank, 2 denotes a first pressure reducing valve, and 3 denotes CO2Flash tank, 4 for a second pressure reducing valve, 5 for CO2A desorption tower.
The following examples and comparative examples are used to provide improved low temperature methanol CO scrubbing2The product gas pressure-raising process is explained in detail.
Example 1:
taking a urea production device producing 40 ten thousand tons of annual products as an example, the low-temperature methanol is washed to absorb CO2The sulfur-free methanol is sent to a sulfur-free methanol flash tank V1603 for medium-pressure flash evaporation, and the pressure of the sulfur-free methanol is 1.85MPaA after flash evaporation; reducing the pressure of the sulfur-free methanol of 1.85MPaA subjected to medium-pressure flash evaporation to 0.60MPaA by using a first pressure reducing valve; 0.60MPaA of sulfur-free methanol was then fed to the CO2Flash drum V1611 flash off, first flash off 0.55MPaA CO2Product gas, CO flashed off2The product gas is subjected to heat exchange, and CO is generated after heat exchange2The pressure of the product gas is0.50MPaA, CO of 0.50MPaA2The product gas is sent into a urea production device CO2Compressor inlet, using CO2Compressor for mixing CO2The product gas is gradually pressurized to about 20MPaA, and then CO of about 20MPaA is added2The product gas is sent into a urea synthesis tower to synthesize urea; CO is discharged by a second pressure reducing valve2Reducing the pressure of the sulfur-free methanol solution flashed by the flash tank to 0.32MPaA, and then sending the sulfur-free methanol solution of 0.32MPaA to CO2The desorption column T1602 desorbs.
CO opened in example 12The compressor is as follows: 4M20 (CO)2The air pumping volume is 75Nm3Min, 1250kW rated power) 1 station, 6MD20 (CO)2Air inflation amount 110Nm3Min, 1850kW rated power) 1.
Comparative example 1:
taking a urea production device producing 40 ten thousand tons of annual products as an example, the low-temperature methanol is washed to absorb CO2The sulfur-free methanol is sent to a sulfur-free methanol flash tank V1603 for medium-pressure flash evaporation, and the pressure of the sulfur-free methanol is 1.85MPaA after flash evaporation; the sulfur-free methanol of 1.85MPaA was depressurized to 0.32MPaA using a second pressure reducing valve, and then the sulfur-free methanol of 0.32MPaA was sent to CO2CO is resolved out by a resolving tower T16022Product gas, CO2The pressure of the product gas after heat exchange and rewarming is 0.25MPaA, and the product gas is sent to a CO production device of urea in an out-of-range area2Compressor inlet, using CO2The compressor gradually increases the pressure to about 20MPaA and then sends the urea to the urea synthesis tower to synthesize the urea.
CO opened in comparative example 12The compressor is as follows: 4M20 (CO)2The air pumping volume is 75Nm3Min, 1250kW rated power) 2 stands, 6MD20 (CO)2Air inflation amount 110Nm3Min, 1850kW rated power) 1.
The gas mass ratio of example 1 and comparative example 1 is shown in table 1.
Table 1: gas mass quantity comparison of example 1 and comparative example 1
| Content providing method and apparatus | Comparative example 1 | Example 1 |
| Pressure (MPaA) | 0.25 | 0.55 |
| Amount (NM3/HR) | 22000 | 22597 |
| Gas composition (mol) | ||
| H2 | 0.005103 | 0.013265 |
| CH4 | 0.000029 | 0.000076 |
| CH4O | 0.000095 | 0.000126 |
| CO | 0.000354 | 0.000963 |
| N2 | 0.000790 | 0.000350 |
| CO2 | 0.993561 | 0.985029 |
| AR | 0.000069 | 0.000190 |
As can be seen from Table 1, the gas quality of example 1 can meet the requirement of urea production without influence.
In comparison to comparative example 1, example 1 utilizes a first pressure reducing valve and CO2Flash tank feeding CO2The pressure of the product gas is increased to 0.55MPaA, thus utilizing CO2Compressor pair CO2When the product gas is pressurized, one compressor can be stopped, one 4M20 compressor is omitted according to the calculation of 50 tons of urea per hour, the electricity consumption of each ton of urea is reduced by about 20 ℃ on the original basis, and the annual effect is about 470 ten thousand yuan.
The features of the embodiments and embodiments described herein above may be combined with each other without conflict.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (6)
1. Improved low-temperature methanol-washing CO2The product gas stripping pressure process is characterized by comprising the following steps:
s1, washing the low-temperature methanol to absorb CO2Feeding the sulfur-free methanol into a sulfur-free methanol flash tank for flash evaporation;
s2, decompressing the sulfur-free methanol flashed in the step S1 by using a first decompression valve;
s3, decreasing the step S2Feeding the pressed sulfur-free methanol into CO2Flash evaporation is carried out by a flash tank;
s4, flashing CO in the step S32The product gas is sent to CO after heat exchange2Compressor inlet, using CO2Compressor pair CO2Pressurizing the product gas, and adding CO after pressurization2The product gas is sent into a urea synthesis tower to synthesize urea; reducing the pressure of the sulfur-free methanol solution flashed in the step S3 by using a second pressure reducing valve, and then sending the reduced pressure sulfur-free methanol solution to CO2Desorbing by using an desorption tower.
2. Improved low temperature methanol CO scrubbing as claimed in claim 12The product gas stripping pressure process is characterized in that in the step S1, after the product gas is flashed by a sulfur-free methanol flash tank, the pressure of the sulfur-free methanol is 1.85 MPaA.
3. Improved low temperature methanol CO scrubbing as claimed in claim 12The product gas stripping pressure process is characterized in that in the step S2, after the pressure is reduced by a first pressure reducing valve, the pressure of the sulfur-free methanol is 0.60 MPaA.
4. Improved low temperature methanol CO scrubbing as claimed in claim 12The product gas stripping and pressing process is characterized in that in step S3, CO is added2After flash evaporation of the flash tank, CO flashed off2The pressure of the product gas was 0.55 MPaA.
5. Improved low temperature methanol CO scrubbing as claimed in claim 12The product gas stripping and pressing process is characterized in that in step S4, CO is added2After the compressor is pressurized, CO2The pressure of the product gas was 20 MPaA.
6. Improved low temperature methanol CO scrubbing as claimed in claim 12And the product gas stripping pressure process is characterized in that in the step S4, after the pressure is reduced by a second pressure reducing valve, the pressure of the sulfur-free methanol solution is 0.32 MpaA.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202010153828.6A CN111420515A (en) | 2020-03-07 | 2020-03-07 | Improved low temperature methanol scrubbing of CO2Product gas stripping and pressing process |
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| CN202010153828.6A CN111420515A (en) | 2020-03-07 | 2020-03-07 | Improved low temperature methanol scrubbing of CO2Product gas stripping and pressing process |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1377825A (en) * | 2001-12-10 | 2002-11-06 | 大连理工大学 | Energy saving raw material gas purifying methanol washing method |
| US20150321136A1 (en) * | 2012-07-20 | 2015-11-12 | Mitsubishi Heavy Industries, Ltd. | Co2 recovery system |
| CN106318475A (en) * | 2015-06-15 | 2017-01-11 | 上海东化环境工程有限公司 | Improvement technology of low temperature methanol washing |
| CN207933375U (en) * | 2018-01-10 | 2018-10-02 | 上海朴力节能环保科技有限公司 | Low-temp methanol washes the device of journey mesohigh recycling carbon dioxide |
-
2020
- 2020-03-07 CN CN202010153828.6A patent/CN111420515A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1377825A (en) * | 2001-12-10 | 2002-11-06 | 大连理工大学 | Energy saving raw material gas purifying methanol washing method |
| US20150321136A1 (en) * | 2012-07-20 | 2015-11-12 | Mitsubishi Heavy Industries, Ltd. | Co2 recovery system |
| CN106318475A (en) * | 2015-06-15 | 2017-01-11 | 上海东化环境工程有限公司 | Improvement technology of low temperature methanol washing |
| CN207933375U (en) * | 2018-01-10 | 2018-10-02 | 上海朴力节能环保科技有限公司 | Low-temp methanol washes the device of journey mesohigh recycling carbon dioxide |
Non-Patent Citations (1)
| Title |
|---|
| 成莉燕 等: "《现代煤化工生产技术》", 31 December 2014, 北京理工大学出版社 * |
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