CN113082947A - Device and method for recovering pressure energy by adopting MDEA decarburization process - Google Patents
Device and method for recovering pressure energy by adopting MDEA decarburization process Download PDFInfo
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- CN113082947A CN113082947A CN202110403561.6A CN202110403561A CN113082947A CN 113082947 A CN113082947 A CN 113082947A CN 202110403561 A CN202110403561 A CN 202110403561A CN 113082947 A CN113082947 A CN 113082947A
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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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- 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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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
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Abstract
The invention discloses a device and a method for recovering pressure energy by adopting an MDEA decarburization process, and the device comprises an absorption tower, a heater HE01, a heater HE02, a primary pressure reducing valve, a primary desorption tower, a secondary pressure reducing valve, a secondary desorption tower and CO which are connected in sequence2The upper part of the absorption tower is sequentially connected with a first air cooler and a high-pressure pump, the other end of the high-pressure pump is connected with the desorption tower, the upper part of the primary desorption tower is connected with a turbine expansion system, and the other end of the turbine expansion system and CO are connected2The discharge/recovery system is connected. The device provided by the invention can recover the capacity loss of MDEA when the MDEA is decompressed from higher pressure to lower pressure, and reduce CO after high-temperature analysis2Gas temperature, reducing downstream CO2The MDEA content in the process finally achieves the purposes of effectively recovering the pressure energy lost in the process and effectively reducing the energy consumption in the process.
Description
Technical Field
The invention relates to the technical field of MDEA decarburization, in particular to a device and a method for recovering pressure energy by adopting an MDEA decarburization process.
Background
In the process of preparing natural gas or coal gas, the generated hydrogen, CO and CO are contained2Etc., in the tail gas, the CO needs to be removed2Hydrogen and CO are fed into a downstream chemical production process. CO currently used2The removing process is mainly an MDEA method.
Containing H after reforming natural gas or making gas from coal2And the mixed gas of CO enters the lower part of the absorption tower under the state of higher pressure and lower temperature, the MDEA solution is pressurized to the process pressure by a high-pressure pump, is cooled to the low-temperature state, enters the upper part of the absorption tower for spraying, and is fully contacted with the mixed gas through a filler layer to absorb the CO in the mixed gas2And water, CO in the gas mixture2After being fully absorbed to reach the design index, the raw materials enter the downstream process. Absorb CO2Heating the MDEA solution to regeneration temperature, decompressing, and introducing into a desorption tower in which CO is introduced2Fully resolving from MDEA solution, and CO at higher temperature2After cooling, the gas is separated from the condensed MDEA and enters a downstream process. Resolving CO2The MDEA high-temperature low-pressure solution is pressurized and cooled by a pump and then enters CO again2The absorption tower forms a closed-loop continuous process.
In the MDEA decarburization process, the absorption capacity of MDEA is positively correlated with pressure, the absorption capacity of MDEA is negatively correlated with temperature, and MDEA needs to be absorbed at higher pressure/lower temperature and is analyzed at lower pressure/higher temperature, so that the absorption tower has higher working pressure and lower temperature, and the analysis tower has lower working pressure and higher temperature. Absorb CO at higher pressure2The MDEA liquid is decompressed by a pressure reducing valve, and the desorbed higher-temperature CO containing MDEA saturated steam2The MDEA in the steam state is condensed by cooling through a cooler, and the MDEA in the steam state after cooling follows CO2Into a downstream process or into the atmosphere.
Disclosure of Invention
The invention aims to provide a device and a method for recovering pressure energy by adopting an MDEA decarburization process, which can recover the capacity loss of MDEA from higher pressure to lower pressure.
In order to achieve the aim, the invention provides a device for recovering pressure energy in an MDEA decarburization process, which comprises an absorption tower, a heater HE01, a heater HE02, a primary pressure reducing valve, a pressure energy recovery device and a pressure energy recovery device which are sequentially connected,Primary stripper, secondary pressure reducing valve, secondary stripper and CO2The upper part of the absorption tower is sequentially connected with a first air cooler and a high-pressure pump, the other end of the high-pressure pump is connected with the desorption tower, the upper part of the primary desorption tower is connected with a turbine expansion system, and the other end of the turbine expansion system and CO are connected2The discharge/recovery system is connected.
The beneficial effect who adopts above-mentioned scheme is: absorption/desorption of CO from MDEA2Characteristic of (1), CO absorbed at high pressure/low temperature2With MDEA/CO2Increase in solution temperature CO2The saturated vapor pressure of (A) gradually increases and absorbed CO2Gradually desorbed CO at high temperature/pressure2The gas potential energy can be recovered through a turbine expansion system, and the recovered energy can be used for generating electricity or directly driving power equipment. Low temperature CO after turboexpansion2The temperature can be controlled by adjusting parameters, and the energy consumption of a subsequent cooler and the MDEA consumption can be effectively reduced.
Further, the upper part, the middle part and the lower part of the primary analysis tower are respectively provided with an air outlet, an air inlet and a liquid outlet.
The beneficial effect who adopts above-mentioned scheme is: gas enters a primary desorption tower from a gas inlet, desorption is carried out in the primary desorption tower, and high-temperature CO is separated2High temperature CO is discharged from the gas outlet2Sending to turbine expansion system, and removing CO2And the MDEA solution enters the secondary desorption tower through a liquid outlet.
Further, the stripper column is connected with CO2And a second air cooler is arranged between the discharge/recovery systems.
The beneficial effect who adopts above-mentioned scheme is: after the desorption tower is subjected to desorption, the CO desorbed from the desorption tower2The gas-liquid separation can be realized by cooling through the air cooler, and then the gas-liquid separation and the CO discharged by the turbine system2Mixing, introducing into CO2A drain/recovery system.
Further, the number of the turbo-expansion systems is one or more.
Further, a sprayer is arranged at the upper part of the absorption tower.
The beneficial effect who adopts above-mentioned scheme is: MDEA solution analyzed from the analysis tower is pressurized by a high-pressure pump, cooled by an air cooler and then can be put into the absorption tower for recycling. The spray thrower can improve MDEA solution and mist area of contact, improves absorption efficiency.
Furthermore, a pipeline connected with the heater HE02 is arranged between the secondary pressure relief valve and the analysis tower, and a bypass pressure relief valve is arranged on the pipeline.
Further, the method for recovering the pressure energy by adopting the device for recovering the pressure energy by the MDEA decarburization process comprises the following steps:
(1) adsorption of CO2
Will contain H2CO and CO2The mixed gas is introduced into the lower part of the absorption tower under the conditions that the pressure range is 1.0-4.0MPa and the temperature range is 40-50 ℃, is mixed with the MDEA solution sprayed by the sprayer, is heated to 100-120 ℃ from the lower part of the absorption tower through a heater HE01 and a heater HE02, is decompressed by a decompression valve and then enters the primary desorption tower;
(2) resolving CO2
In the primary desorption tower, the temperature range of the desorbed CO is higher than 100-120 DEG C2CO entering a turbine expansion system and having a temperature range of less than 100 ℃ and 120 DEG C2And the MDEA mixed solution enters a secondary desorption tower through secondary decompression;
(3) gas-liquid separation
The solution entering the secondary desorption tower undergoes desorption and gas-liquid separation, and CO2Cooling by a second air cooler to remove liquid MDEA, and introducing into CO2A discharge/recovery system;
(4) recovering pressure energy
CO separated from the primary stripper2After entering a turbine expansion system and being subjected to energy recovery, the CO is separated from CO separated in a separation tower2Mixing and introducing into CO2A drain/recovery system.
The beneficial effect who adopts above-mentioned scheme is: from MDEA/CO2The high-pressure solution of the absorption tower enters a newly added primary desorption tower after being heated and decompressed, and high-temperature CO is desorbed2Energy recovery into the newly added turbine system is lowWarm CO2After gas-liquid separation and removal of liquid MDEA, the downstream process is carried out; MDEA/CO effluent from primary stripper2The solution enters a secondary desorption tower after secondary decompression, and CO is finally finished2Resolving, CO resolved2Cooling, gas-liquid separating, and mixing with CO discharged from turbine expansion system2Mixing and entering a downstream process.
In summary, the invention has the following advantages:
1. the method for recovering the pressure energy by the MDEA decarburization process of the natural gas/coal chemical gas making process can realize long-term high-efficiency operation and continuously recover the energy lost in the process;
2. reduce CO after analysis2The temperature of the MDEA is effectively reduced;
3. the system is simple to operate, so that automatic operation can be realized without increasing operators;
4. and a system operation stability guarantee system is arranged to ensure continuous and stable operation of the system.
Drawings
FIG. 1 is a schematic flow diagram of the pressure energy recovery of the MDEA decarburization process provided by the present invention;
FIG. 2 is MDEA vs. CO at different pressures2The absorption capacity of (c);
FIG. 3 shows MDEA absorption of CO at a recycle rate of 500 tons2The generated energy of the pressure energy is shown schematically.
Detailed Description
The principles and features of this invention are described below in conjunction with embodiments, which are included to explain the invention and not to limit the scope of the invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
As shown in figure 1, the invention provides a device for recovering pressure energy by adopting an MDEA decarburization process, which comprises an absorption tower, a heater HE01, a heater HE02, a primary pressure reducing valve PVC01, a primary desorption tower, a secondary pressure reducing valve PVC02, a secondary desorption tower and CO which are connected in sequence2The upper part of the absorption tower is sequentially connected with a first air cooler and a high-pressure pump, the other end of the high-pressure pump is connected with a secondary desorption tower, the upper part of the primary desorption tower is connected with a turbine expansion system, and the other end of the turbine expansion system and CO are connected2The discharge/recovery system is connected. The turbine expansion system is provided with a power output interface, the power output interface of the turbine expansion system can be connected with an engine to drive a generator to generate electricity, and the power output interface of the turbine expansion system can also directly drive equipment to operate.
Wherein, the upper part of the middle analysis tower is provided with an air outlet, the middle part of the middle analysis tower is provided with an air inlet, and the lower part of the middle analysis tower is provided with a liquid outlet; secondary desorption column with CO2A second air cooler is arranged between the discharge/recovery systems; the number of the turboexpansion systems is one or more; a sprayer is arranged at the upper part of the absorption tower; a pipeline connected with the heater HE02 is arranged between the secondary decompression valve PVC02 and the secondary desorption tower, and a bypass decompression valve PVC03 is arranged on the pipeline.
The method for recovering the pressure energy by adopting the device for recovering the pressure energy by the MDEA decarburization process in a certain chemical plant comprises the following steps:
(1) adsorption of CO2
Will contain H2CO and CO2The mixed gas is introduced into the lower part of the absorption tower under the conditions that the pressure range is 3.2MPa and the temperature range is 45 ℃, is mixed with MDEA solution sprayed out by a sprayer, is decompressed by a primary decompression valve PVC01 from the lower part of the absorption tower and then enters a primary desorption tower;
(2) resolving CO2
In the primary desorption tower, CO desorbed in the temperature range higher than 110 DEG C2CO entering a turbine expansion system and having a temperature range below 110 DEG C2And the MDEA mixed solution enters a secondary desorption tower through secondary decompression;
(3) gas-liquid separation
The solution in the secondary desorption tower is subjected to desorption and gas-liquid separation, and CO2Cooling by a second air cooler to remove liquid MDEA, and introducing into CO2A discharge/recovery system;
(4) recovering pressure energy
CO separated from the primary stripper2After entering a turbine expansion system and being subjected to energy recovery, the CO is separated from CO separated in a separation tower2Mixing and introducing into CO2A drain/recovery system.
Wherein the MDEA circulation amount is about 500ton/h, and the absorbed CO is2About 40 tons/h, the working pressure of the absorption tower is 3.2MPa, the absorption temperature is 45 ℃, the desorption temperature of the desorption tower is 110 ℃, the desorption pressure is 0.12MPa, and the power consumption of the MDEA circulating high-pressure pump is about 900 kW. The device and the method for recovering the pressure energy by adopting the MDEA decarburization process provided by the invention are used for testing the CO under different pressures under the temperature condition of 110-2Absorption capacity, the data obtained are shown in figure 2; by the data in FIG. 2, the CO content in the range of 1.0-3.2MPa, 110-2The relationship between the amount and the expansion energy is analyzed, and a power generation amount curve can be obtained through comparison of test data, as shown in fig. 3. As can be seen from FIG. 3, by using different recovery parameters and by using the analysis of the turbine pressure energy recovery test data, the energy consumption of about 700-1000kW can be saved, and under the condition that the optimal parameter, i.e., the pressure is 2.0MPa, the recovery power can reach 900-1000 kW.
While the present invention has been described in detail with reference to the illustrated embodiments, it should not be construed as limited to the scope of the present patent. Various modifications and changes may be made by those skilled in the art without inventive step within the scope of the appended claims.
Claims (5)
1. The device for recovering pressure energy by adopting the MDEA decarburization process is characterized by comprising an absorption tower, a heater HE01, a heater HE02, a primary pressure reducing valve, a primary desorption tower, a secondary pressure reducing valve, a secondary desorption tower and CO which are sequentially connected2The upper part of the absorption tower is sequentially connected with a first air cooler and a high-pressure pump, the other end of the high-pressure pump is connected with the secondary desorption tower, the upper part of the primary desorption tower is connected with a turbine expansion system, and the other end of the turbine expansion system and CO are connected2DischargingRecovery system connection.
2. The apparatus for recovering pressure energy using MDEA decarburization process as claimed in claim 1, wherein the upper part, the middle part and the lower part of the primary stripper are provided with a gas outlet, a gas inlet and a liquid outlet, respectively.
3. The apparatus for recovering pressure energy using an MDEA decarbonization process of claim 1, wherein the number of the turbo-expansion systems is at least one.
4. The apparatus for recovering pressure energy using an MDEA decarbonization process of claim 1, wherein the turboexpansion system is configured with a power take-off interface, the power take-off interface being connected to an engine or a connection device.
5. The method for recovering pressure energy by using the device for recovering pressure energy by using the MDEA decarburization process, as recited in any one of claims 1 to 4, comprising the steps of:
(1) adsorption of CO2
Will contain H2CO and CO2The mixed gas is introduced into the lower part of the absorption tower under the conditions that the pressure range is 1.0-4.0MPa and the temperature range is 40-50 ℃, is mixed with the MDEA solution, is heated to 100-120 ℃ from the lower part of the absorption tower through a heater HE01 and a heater HE02, is decompressed by a primary pressure reducing valve and then enters a primary desorption tower;
(2) resolving CO2
In the primary desorption tower, the temperature range of the desorbed CO is higher than 100-120 DEG C2Entering a turboexpansion system, and unassociated CO2And the MDEA solution enters a secondary desorption tower through secondary decompression;
(3) gas-liquid separation
The solution entering the secondary desorption tower undergoes desorption and gas-liquid separation, and CO2Cooling by a second air cooler to remove liquid MDEA, and introducing into CO2A discharge/recovery system;
(4) recovering pressure energy
CO separated from the primary stripper2After entering a turbine expansion system and being subjected to energy recovery, the CO is separated from CO separated in a separation tower2Mixing and introducing into CO2A drain/recovery system.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101616725A (en) * | 2007-02-28 | 2009-12-30 | 株式会社日立工业设备技术 | The processing of oxidation reaction flue gas and energy reclaiming method |
| US20120255305A1 (en) * | 2011-04-06 | 2012-10-11 | Mitsubishi Heavy Industries, Ltd. | Carbon dioxide recovery system and method |
| CN102876412A (en) * | 2012-09-14 | 2013-01-16 | 郑州大学生化工程中心 | Energy-saving decarbonization process for biogas |
| JP2013151876A (en) * | 2012-01-24 | 2013-08-08 | Toshiba Corp | Carbon dioxide separation recovery device, carbon dioxide recovery type steam power generation system, and method for operating the same |
| US20150376801A1 (en) * | 2013-02-21 | 2015-12-31 | Faramarz Bairamijamal | High pressure process for CO2 capture, utilization for heat recovery, power cycle, super-efficient hydrogen based fossil power generation and conversion of liquid CO2 with water to syngas and oxygen |
| CN105268283A (en) * | 2015-09-28 | 2016-01-27 | 北京化工大学 | Combined absorption carbon dioxide trapping and compressing treatment technology |
| CN106016854A (en) * | 2016-06-29 | 2016-10-12 | 湖北三宁化工股份有限公司 | PC decarbonization process PC liquid pressure energy recovery method and device |
| CN109200757A (en) * | 2018-09-05 | 2019-01-15 | 中石化上海工程有限公司 | The method of natural gas ethylene unit pressure recovery energy |
-
2021
- 2021-04-15 CN CN202110403561.6A patent/CN113082947B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101616725A (en) * | 2007-02-28 | 2009-12-30 | 株式会社日立工业设备技术 | The processing of oxidation reaction flue gas and energy reclaiming method |
| US20120255305A1 (en) * | 2011-04-06 | 2012-10-11 | Mitsubishi Heavy Industries, Ltd. | Carbon dioxide recovery system and method |
| JP2013151876A (en) * | 2012-01-24 | 2013-08-08 | Toshiba Corp | Carbon dioxide separation recovery device, carbon dioxide recovery type steam power generation system, and method for operating the same |
| CN102876412A (en) * | 2012-09-14 | 2013-01-16 | 郑州大学生化工程中心 | Energy-saving decarbonization process for biogas |
| US20150376801A1 (en) * | 2013-02-21 | 2015-12-31 | Faramarz Bairamijamal | High pressure process for CO2 capture, utilization for heat recovery, power cycle, super-efficient hydrogen based fossil power generation and conversion of liquid CO2 with water to syngas and oxygen |
| CN105268283A (en) * | 2015-09-28 | 2016-01-27 | 北京化工大学 | Combined absorption carbon dioxide trapping and compressing treatment technology |
| CN106016854A (en) * | 2016-06-29 | 2016-10-12 | 湖北三宁化工股份有限公司 | PC decarbonization process PC liquid pressure energy recovery method and device |
| CN109200757A (en) * | 2018-09-05 | 2019-01-15 | 中石化上海工程有限公司 | The method of natural gas ethylene unit pressure recovery energy |
Non-Patent Citations (1)
| Title |
|---|
| 赵会军等: "热泵应用于MDEA再生系统的可行性分析", 《天然气化工(C1化学与化工)》 * |
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