CN109200758B - Method for recovering pressure energy of ethylene device - Google Patents
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- CN109200758B CN109200758B CN201811031330.1A CN201811031330A CN109200758B CN 109200758 B CN109200758 B CN 109200758B CN 201811031330 A CN201811031330 A CN 201811031330A CN 109200758 B CN109200758 B CN 109200758B
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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
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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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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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- C07C7/005—Processes comprising at least two steps in series
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
- C10G70/06—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
- B01D2252/20484—Alkanolamines with one hydroxyl group
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
- B01D2252/20489—Alkanolamines with two or more hydroxyl groups
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
The invention relates to a method for recovering pressure energy of an ethylene device, which mainly solves the problems of high energy consumption and high power and electricity charges in the prior art. The invention adopts a method for recovering pressure energy by an ethylene device, a pressure recovery device is additionally arranged between an absorption tower and a desorption tower, a high-temperature rich liquid absorbent is converted into a low-pressure rich liquid absorbent from high pressure, and a low-pressure barren liquid absorbent from the bottom of the desorption tower is converted into a high-pressure barren liquid absorbent from low pressure, so that the technical scheme of saving external energy and power cost better solves the problems and can be used in the ethylene device.
Description
Technical Field
The invention relates to a method for recovering pressure energy of an ethylene device.
Background
The steam thermal cracking is the most mature olefin production technology, and adopts petroleum cracking raw materials to produce carbon chain breakage or dehydrogenation reaction under the high-temperature condition to produce ethylene and propylene products, and simultaneously can obtain butylene, butadiene and byproducts such as pyrolysis gasoline, pyrolysis diesel oil, pyrolysis fuel oil and the like. The ethylene device is a typical petrochemical large-scale commercial industrial production device for preparing ethylene by adopting a steam thermal cracking method, the content of acid gases such as hydrogen sulfide H2S and carbon dioxide CO2 in cracked gas flowing out of a cracking furnace is 0.02-0.19 mol%, and in order to prepare polymer-grade ethylene and polymer-grade propylene, the hydrogen sulfide H2S and the carbon dioxide CO2 in the cracked gas are generally required to be removed and are respectively reduced to below 2.0 ppm. In the prior art, an alkaline washing method is usually adopted to remove acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2, from cracked gas of an ethylene unit, when the contents of the acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2 are too high, in order to reduce the alkali consumption, a reproducible ethanol amine method solvent is adopted to absorb and remove most of the acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2, and then an alkaline washing method is adopted to further remove the rest of the acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2, so that the acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2, in the cracked gas are removed to be below 2 ppm. When absorbing acid gases of hydrogen sulfide H2S and carbon dioxide CO2 by an ethanolamine method, the process parameters adopt low temperature and high pressure, and an absorbent can absorb and dissolve a large amount of acid gases to become a rich liquid absorbent; when desorbing acid gases such as hydrogen sulfide H2S and carbon dioxide CO2, the process parameters adopt high temperature and low pressure, and the absorbent can desorb and release a large amount of acid gases to become a barren solution absorbent. Therefore, the acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2, in the cracked gas of the ethylene plant are separated by the absorbents with different process parameters, and the absorbents can be repeatedly recycled.
In the prior art, CN200910212788.1 discloses a method for deeply removing carbon dioxide from a gas mixture. A composite amine aqueous solution is used as an absorbent, raw gas containing 22 vol% is subjected to absorption treatment for removing carbon dioxide, and the carbon dioxide content of the purified mixed gas is reduced to 0.04-0.80 vol%. CN 201310149170.1 discloses a method for removing hydrogen sulfide from crude carbon dioxide by using a heat pump circulation method. CN201610404569.3 sea water desalination waste water pressure recovery device discloses sea water desalination waste water pressure utilization and pressure recovery method, has reached energy saving and emission reduction's purpose.
In the unit process technology of removing the hydrogen sulfide H2S and the carbon dioxide CO2 in the acid gas of the cracked gas by the ethylene device, in the process of separating the hydrogen sulfide H2S and the carbon dioxide CO2 in the acid gas of the cracked gas by adopting the absorbents with different pressure and temperature process parameters, the absorbents need to be recycled. When the high-pressure rich liquid absorbent is recycled, the high-pressure rich liquid absorbent at the tower bottom outlet of the high-pressure absorption tower is decompressed by a pressure reducing valve and then is sent to the tower top inlet of the low-pressure desorption tower, and the pressure energy of the rich liquid absorbent is wasted; the low-pressure barren liquor absorbent at the bottom outlet of the low-pressure desorption tower can be sent to the top inlet of the high-pressure absorption tower after being pressurized by external input energy, and the pressurization of the barren liquor absorbent has to be realized by external input energy.
CN200910212788.1 and CN 201310149170.1 only disclose technical solutions for removing acid gases, hydrogen sulfide H2S and carbon dioxide CO2, there is no technical method for pressure recovery in the process of removing acid gases by an ethylene plant, and there is no technical means for pressure recovery of the existing pressure energy by a pressure recovery plant, CN201610404569.3 is only a technical solution and a process route for pressure recovery, there is no technical means for specific engineering implementation, and it cannot be applied to an ethylene plant in an industrial production scale. Therefore, in the operation process of the unit for removing the acid impurities in the cracked gas by the ethylene device in the prior art, the problems of high operation energy consumption and high power electricity charge exist.
Disclosure of Invention
The invention aims to solve the technical problems of high energy consumption and high power electricity cost in the prior art, and provides a novel method for recovering pressure energy by an ethylene device, which has the advantages of low energy consumption and low power electricity cost.
In order to solve the problems, the technical scheme adopted by the invention is as follows: a method for recovering pressure energy of an ethylene plant comprises the following steps:
(a) the method comprises the following steps that (1) quenched and compressed cracking gas 11 flowing out of an out-of-range ethylene cracking furnace enters the bottom of an absorption tower 1, meanwhile, a low-temperature barren solution absorbent 23 with reduced temperature and increased pressure enters the top of the absorption tower 1, the cracking gas 11 is in countercurrent contact with the low-temperature barren solution absorbent 23 in the absorption tower 1, acid gas in the cracking gas 11 is absorbed by the low-temperature barren solution absorbent 23, and purified cracking gas 12 with acid gas removed flows out of the top of the absorption tower 1 and is sent out of the range;
(b) the high-pressure rich liquid absorbent 13 for absorbing the acid gas flows out of the bottom of the absorption tower 1, and is subjected to heat exchange by the lean rich absorbent heat exchanger 2 to be heated into a high-temperature rich liquid absorbent 14; under normal working conditions, the valve of the bypass pipeline 25 is closed, and the high-temperature rich liquid absorbent 14 flows to the high-temperature rich liquid absorbent 15 and enters the inlet of the pressure reduction end of the pressure recovery device 3;
(c) under normal working conditions, the high-temperature rich liquid absorbent 15 enters the inlet of the pressure reduction end of the pressure recovery device 3, the pressure of the high-temperature rich liquid absorbent 15 is converted from high pressure to low pressure, and the low-pressure rich liquid absorbent 16 flowing out of the pressure recovery device 3 flows to the low-pressure rich liquid absorbent 17 and enters the top of the desorption tower 6;
(d) the low-pressure rich liquid absorbent 17 is sent to the top of the desorption tower 6, and direct steam 19 is supplied to the outside and enters the bottom of the desorption tower 6; in the desorption tower 6, external direct steam 19 is supplied to reduce the partial pressure of the low-pressure rich liquid absorbent 17 and increase the temperature of the low-pressure rich liquid absorbent 17, the rich liquid absorbent 17 is in countercurrent contact with the external direct steam 19 to carry out gas stripping regeneration, acid gas in the rich liquid absorbent 17 is desorbed by the external direct steam 19, and the acid gas 18 flows out of the top of the desorption tower 6 and is sent out;
(e) the low-pressure barren solution absorbent 20 for removing the acid gas flows out from the bottom of the desorption tower 6; under normal working conditions, inlet valves and outlet valves of the standby booster pump 4 and the standby booster pump 4 of the bypass pipeline 24 are closed, and the low-pressure lean liquid absorbent 20 enters the pre-booster pump 5 for boosting and then becomes a low-pressure lean liquid absorbent 21 and enters an inlet of a boosting end of the pressure recovery device 3;
(f) the high-temperature rich liquid absorbent 15 enters the inlet of the pressure reduction end of the pressure recovery device 3, and the low-pressure lean liquid absorbent 21 enters the inlet of the pressure boosting end of the pressure recovery device 3; in the pressure recovery device 3, the pressure energy of the high-temperature rich liquid absorbent 15 at the high-pressure side of the decompression end is converted into mechanical energy of the rotating shaft and then converted into the pressure energy of the low-pressure lean liquid absorbent 21 at the low-pressure side of the boosting end, the pressure of the low-pressure lean liquid absorbent 21 is increased and converted into the high-pressure lean liquid absorbent 22, and the pressure meets the pressure required by the absorption operation of the absorption tower 1, so that the output pressure of the preposed booster pump 5 is reduced, and the power consumption of a motor is reduced;
(g) under normal working conditions, the low-pressure barren solution absorbent 21 enters an inlet at a boosting end of the pressure recovery device 3, the pressure of the low-pressure barren solution absorbent 21 is converted from low pressure to high pressure in the pressure recovery device 3, the high-pressure barren solution absorbent 22 flowing out of the pressure recovery device 3 flows to the poor and rich absorbent heat exchanger 2 to exchange heat and reduce the temperature, and the low-temperature barren solution absorbent 23 after being cooled returns to enter the top of the absorption tower 1 to be recycled for absorbing acid gas in the cracked gas 11;
the pressure recovery device 3 is an online pressure recovery device adopting a hydraulic turbine principle, a pressure reduction end high-pressure side impeller and a pressure boosting end low-pressure side impeller are directly connected in the same pump body through a rotating shaft, a high-pressure rich liquid absorbent at a pressure reduction end drives the pressure reduction end high-pressure side impeller, the pressure boosting end low-pressure side impeller is driven to rotate through the rotating shaft, the pressure of a low-pressure lean liquid absorbent at a pressure boosting end is increased, and therefore the pressure energy at the pressure reduction end high-pressure side is converted into the mechanical energy of the rotating shaft and then converted into the pressure energy at the pressure boosting end low-pressure side, and the rotating shaft in the pressure recovery device 3 is the only operating part, so that the pressure recovery device 3 has no shaft seal and no additional lubricating system.
In the above technical solution, preferably, when the pressure recovery device 3 has a fault condition, the valve in the bypass closed state when the pressure recovery device 3 is in the normal condition is opened and the backup booster pump 4 is opened at the same time, the high-temperature rich liquid absorbent 14 is sent from the lean rich absorbent heat exchanger 2 to the top of the desorption tower 6 through the pipeline 25, and the low-pressure lean liquid absorbent 20 is pressurized to the top of the absorption tower 1 through the pipeline 24 and the backup booster pump 4; starting the operation condition without using the pressure recovery device 3, thereby ensuring the normal circulating operation of the absorbent between the absorption tower 1 and the desorption tower 6.
In the technical scheme, preferably, the mole fraction of the acid-containing gas in the cracking gas 11 entering the bottom of the absorption tower 1 is 0.02-0.19%; the mole fraction of acid-containing gas in the purified cracked gas 12 flowing out of the top of the absorption tower 1 is less than or equal to 2.0 ppm; the acid gases were hydrogen sulfide H2S and carbon dioxide CO 2.
In the technical scheme, preferably, the operating pressure range of the absorption tower 1 is 1.5-2.5 MPa, the tower top operating temperature range is 55-72 ℃, and the tower bottom operating temperature range is 58-75 ℃.
In the above technical scheme, preferably, the absorption tower 1 adopts monoethanolamine MEA with a mole fraction of 15-20% or diethanolamine DEA with a mole fraction of 25-35% as an absorbent.
In the technical scheme, preferably, the operating pressure of the desorption tower 6 ranges from 0.1MPa to 1.1MPa, the operating temperature of the top of the tower ranges from 100 ℃ to 115 ℃, and the operating temperature of the bottom of the tower ranges from 104 ℃ to 119 ℃.
In the technical scheme, the desorption tower 6 preferably adopts the externally supplied direct steam 19 with the operating pressure ranging from 0.2MPa to 1.2MPa and the operating temperature ranging from 140 ℃ to 208 ℃.
In the above technical scheme, preferably, the pressure recovery device 3 has an inlet operation pressure range of 1.5-2.5 MPa at the pressure reduction end and an outlet operation pressure range of 0.4-1.4 MPa; the inlet operating pressure range of the boosting end is 0.9-1.9 MPa, and the outlet operating pressure range is 1.9-2.9 MPa.
In the above technical scheme, preferably, the pre-booster pump 5 is started, the inlet operating pressure range is 0.1-1.1 MPa, and the outlet operating pressure range is 0.9-1.9 MPa.
The invention relates to a method for recovering pressure energy of an ethylene device, and for the ethylene device with the production scale of 11.5-150 million tons/year, a pressure recovery device 3 is additionally arranged between an absorption tower 1 and a desorption tower 6, a high-temperature rich liquid absorbent 15 is converted into a low-pressure rich liquid absorbent 16 from high pressure, and a low-pressure lean liquid absorbent 21 from the bottom of the desorption tower 6 is converted into a high-pressure lean liquid absorbent 22 from low pressure, so that the external energy supply is saved by more than 60.14-65.61%, the electric power cost is saved by more than 12-143 million yuan/year, and a better technical effect is obtained.
Drawings
FIG. 1 is a schematic flow diagram of the process of the present invention.
In FIG. 1, 1-absorber column; 2-lean rich absorbent heat exchanger; 3-a pressure recovery device; 4-standby booster pump; 5-a pre-booster pump; 6-a desorber; 11-cracked gas; 12-purifying the cracked gas; 13-high pressure rich liquid absorbent; 14-high temperature rich liquid absorbent; 15-high temperature rich liquid absorbent; 16-low pressure rich liquid absorbent; 17-low pressure rich liquid absorbent; 18-acid gases hydrogen sulfide H2S and carbon dioxide CO 2; 19-external supply of direct steam; 20-low pressure lean liquid absorbent; 21-low pressure lean liquid absorbent; 22-high pressure lean liquid absorbent; 23-a low temperature lean liquor absorbent; 24-a low pressure lean liquid absorbent bypass line; 25-high temperature rich liquid absorbent bypass line.
The present invention will be further illustrated by the following examples, but is not limited to these examples.
Detailed Description
Comparative example 1
Taking production scale 11.5 million tons/year, 30 million tons/year, 70 million tons/year, 80 million tons/year, 100 million tons/year and 150 million tons/year ethylene units as examples respectively, the ethylene units adopt the prior art, and in the process of removing acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2, the pressure recovery technology is not adopted, and the pressure energy recovery through the pressure recovery device and the power consumption and the economic benefit of a deacidification absorbent conveying pump are not considered, which are shown in Table 1.
TABLE 1 summary of power consumption and economic benefits of delivery pumps
| Production scale (ten thousand tons/year) | 11.5 | 30 | 70 | 80 | 100 | 150 |
| Power consumption of delivery pump (kilowatt) | 28.08 | 67.88 | 167.90 | 193.06 | 253.83 | 379.24 |
| Delivery pump motor power (kilowatt) | 40 | 90 | 210 | 240 | 300 | 440 |
| Calculating Motor efficiency (%) | 70.21 | 75.42 | 79.95 | 80.44 | 84.61 | 86.19 |
| Annual electric power consumption (kilowatt-hour) | 320000 | 720000 | 1680000 | 1920000 | 2400000 | 3520000 |
| Annual electric power charge (Wanyuan) | 20 | 44 | 104 | 118 | 148 | 217 |
[ example 1 ]
Taking a production scale 11.5 ten thousand tons/year ethylene plant as an example, the method for recovering pressure energy by using the ethylene plant of the invention is shown in figure 1, and the process flow is as follows: the method comprises the steps that a pyrolysis gas 11 which flows out of an outside ethylene cracking furnace and is quenched and compressed enters the bottom of an absorption tower 1, meanwhile, a low-temperature barren solution absorbent 23 with reduced temperature and increased pressure enters the top of the absorption tower 1, the pyrolysis gas 11 is in countercurrent contact with the low-temperature barren solution absorbent 23 in the absorption tower 1, acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2 in the pyrolysis gas 11 are absorbed by the low-temperature barren solution absorbent 23, and a purified pyrolysis gas 12 with acid gas removed flows out of the top of the absorption tower 1 and is sent to the outside. The high-pressure rich liquid absorbent 13 for absorbing acid gases of hydrogen sulfide H2S and carbon dioxide CO2 flows out from the bottom of the absorption tower 1, is subjected to heat exchange by the lean rich absorbent heat exchanger 2 to be heated to be the high-temperature rich liquid absorbent 14, the high-temperature rich liquid absorbent 14 flows to the high-temperature rich liquid absorbent 15 to enter the inlet of the pressure reduction end of the pressure recovery device 3, and the pressure of the high-temperature rich liquid absorbent 15 is converted from high pressure to the low-pressure rich liquid absorbent 16. The low-pressure rich liquid absorbent 16 flowing out of the pressure recovery device 3 flows to the low-pressure rich liquid absorbent 17 to enter the top of the desorption tower 6, and the external direct steam 19 enters the bottom of the desorption tower 6. In the desorption tower 6, the partial pressure of the low-pressure rich liquid absorbent 17 is reduced by the externally supplied direct steam 19, the temperature of the low-pressure rich liquid absorbent 17 is increased, the rich liquid absorbent 17 is in countercurrent contact with the externally supplied direct steam 19 for stripping regeneration, the acidic gases of hydrogen sulfide H2S and carbon dioxide CO2 in the rich liquid absorbent 17 are released and desorbed by the externally supplied direct steam 19, and the acidic gas 18 flows out of the top of the desorption tower 6 and is sent to the outside. The low-pressure lean liquid absorbent 20 from which the acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2, are removed flows out from the bottom of the desorption tower 6, enters the pre-booster pump 5 for boosting, and then becomes the low-pressure lean liquid absorbent 21 and enters the inlet of the boosting end of the pressure recovery device 3. In the pressure recovery device 3, the pressure of the low-pressure lean liquid absorbent 21 is converted from low pressure to high pressure, the high-pressure lean liquid absorbent 22 flowing out of the pressure recovery device 3 flows to the lean rich absorbent heat exchanger 2 to exchange heat and reduce the temperature, and the low-temperature lean liquid absorbent 23 after temperature reduction returns to the top of the absorption tower 1 to be recycled for reuse, so that the acid gases, namely hydrogen sulfide H2S and carbon dioxide CO2, in the cracked gas 11 are absorbed again. When the pressure recovery device 3 fails, the bypass valve and the spare booster pump 4 are simultaneously opened, the high-temperature rich liquid absorbent 14 flows from the lean rich absorbent heat exchanger 2 to the top of the desorption tower 6 through the pipeline 25, and the low-pressure lean liquid absorbent 20 flows to the top of the absorption tower 1 after being pressurized through the pipeline 24 and the spare booster pump 4.
The cracking raw materials adopted by the ethylene device are 48% of naphtha, 39% of hydrogenation tail oil and 13% of light hydrocarbon, the cracking gas flowing out of the cracking furnace and entering the separation unit has the composition shown in table 2.
TABLE 2 cracked gas composition List for the separation units
| Component name | Hydrogen | Methane | Carbon monoxide | Hydrogen sulfide | Carbon dioxide | Ethylene |
| Yield/mol% | 15.27 | 21.38 | 0.08 | 0.01 | 0.01 | 31.56 |
| Component name | Carbon two | Propylene (PA) | Carbon III | Carbon four | Carbon five | Water (W) |
| Yield/mol% | 6.67 | 9.50 | 0.90 | 4.66 | 4.74 | 5.22 |
The technological parameters are as follows: the pyrolysis gas 11 entering the bottom of the absorption tower 1 contains acid gas hydrogen sulfide H2S and carbon dioxide CO2 with the mole fraction of 0.02 percent; the purified cracking gas 12 flowing out of the top of the absorption tower 1 contains acid gas hydrogen sulfide H2S and carbon dioxide CO2 with the mole fraction less than or equal to 2.0 ppm. The operation pressure of the absorption tower 1 is 1.8MPa, the operation temperature of the top of the tower is 60 ℃, and the operation temperature of the bottom of the tower is 64 ℃. The absorption tower 1 adopts monoethanolamine MEA with the mole fraction of 17 percent as an absorbent. The operating pressure of the desorption tower 6 is 0.4MPa, the operating temperature of the top of the tower is 106 ℃, and the operating temperature of the bottom of the tower is 110 ℃. The desorption tower 6 adopts the external supply direct steam to operate at the pressure of 0.5MPa and the operating temperature of 172 ℃. The inlet operating pressure of the pressure reduction end of the pressure recovery device 3 is 1.8MPa, and the outlet operating pressure is 0.7 MPa; the inlet operating pressure of the boosting end is 1.2MPa, and the outlet operating pressure is 2.2 MPa. The preposed booster pump 5 is started, the inlet operation pressure is 0.4MPa, and the outlet operation pressure is 1.2 MPa.
The method for recovering the pressure energy by the ethylene device relatively saves the external supply energy by 60.14 percent, saves the electric power cost by 12 ten thousand yuan per year, and obtains other technical effects and economic benefits shown in Table 5.
[ example 2 ]
Similarly [ example 1 ], the production scale was changed to a 30 ten thousand ton/year ethylene plant, the cracking feedstock was changed to 100% heavy naphtha, and the composition of the cracked gas entering the separation unit was changed accordingly, as shown in table 3.
TABLE 3 cracked gas composition List for the separation units
| Component name | Methane hydrogen | Carbon dioxide | Ethylene | Carbon two | Propylene (PA) | Carbon III | Carbon four | Heavy fraction | Total up to |
| Yield/wt% | 14.00 | 0.15 | 19.90 | 3.10 | 12.00 | 0.10 | 8.10 | 42.65 | 100.00 |
The technological parameters are as follows: the mass fraction of the cracked gas 11 entering the bottom of the absorption tower 1 and containing acidic gas carbon dioxide CO2 is 0.15%; the mole fraction of the purified cracked gas 12 flowing out of the top of the absorption tower 1 and containing acid gas carbon dioxide CO2 is less than or equal to 2.0 ppm. The operation pressure of the absorption tower 1 is 1.9MPa, the operation temperature of the top of the tower is 62 ℃, and the operation temperature of the bottom of the tower is 64 ℃. The absorption tower 1 adopts 28 percent of diethanolamine DEA as an absorbent. The operating pressure of the desorption tower 6 is 0.5MPa, the operating temperature of the top of the tower is 107 ℃, and the operating temperature of the bottom of the tower is 111 ℃. The desorption tower 6 adopts the external supply direct steam to operate the pressure of 0.6MPa and the operating temperature of 179 ℃. The inlet operating pressure of the pressure reduction end of the pressure recovery device 3 is 1.9MPa, and the outlet operating pressure is 0.8 MPa; the inlet operating pressure of the boosting end is 1.3MPa, and the outlet operating pressure is 2.3 MPa. The preposed booster pump 5 is started, the inlet operation pressure is 0.5MPa, and the outlet operation pressure is 1.3 MPa.
By adopting the method for recovering the pressure energy by the ethylene device, 61.26% of externally supplied energy is relatively saved, the electric power cost is saved by 27 ten thousand yuan/year, and other obtained technical effects and economic benefits are shown in Table 5.
[ example 3 ]
Similarly [ example 1 ], the cracking feedstock was changed to 100% ethane and the composition of the cracked gas entering the separation unit was changed accordingly, only by changing the production scale to a 70 ten thousand ton/year ethylene plant, see table 4.
TABLE 4 cracked gas composition List for the separation units
| Component name | Methane hydrogen | Acid gas | Ethylene | Carbon two | Propylene (PA) | Carbon four | Heavy fraction | Water (W) | Total up to |
| Yield/vol% | 38.39 | 0.19 | 31.51 | 24.54 | 0.76 | 0.18 | 0.09 | 4.34 | 100.00 |
The technological parameters are as follows: the pyrolysis gas 11 entering the bottom of the absorption tower 1 contains acid gas hydrogen sulfide H2S and carbon dioxide CO2 with the mole fraction of 0.19%; the purified cracking gas 12 flowing out of the top of the absorption tower 1 contains acid gas hydrogen sulfide H2S and carbon dioxide CO2 with the mole fraction less than or equal to 2.0 ppm. The operation pressure of the absorption tower 1 is 2.0MPa, the operation temperature of the top of the tower is 63 ℃, and the operation temperature of the bottom of the tower is 68 ℃. The absorption tower 1 adopts a mixed solution of monoethanolamine MEA with a mole fraction of 16% and diethanolamine DEA with a mole fraction of 27%. The operating pressure of the desorption tower 6 is 0.6MPa, the operating temperature of the top of the tower is 108 ℃, and the operating temperature of the bottom of the tower is 113 ℃. The desorption tower 6 adopts the external supply direct steam to operate at the pressure of 0.7MPa and the operation temperature of 185 ℃. The inlet operating pressure of the pressure reduction end of the pressure recovery device 3 is 2.0MPa, and the outlet operating pressure is 0.9 MPa; the inlet operating pressure of the boosting end is 1.4MPa, and the outlet operating pressure is 2.4 MPa. The preposed booster pump 5 is started, the inlet operation pressure is 0.6MPa, and the outlet operation pressure is 1.4 MPa.
By adopting the method for recovering the pressure energy by the ethylene device, the external supply energy is relatively saved by 62.87%, the electric power cost is saved by 65 ten thousand yuan/year, and other obtained technical effects and economic benefits are shown in Table 5.
[ example 4 ]
Similarly, in example 1, only the production scale was changed to 80 ten thousand tons/year of ethylene process equipment, and by using the method for recovering pressure energy by using the ethylene plant of the present invention, the external energy supply was relatively saved by 63.41%, the electric power cost was saved by 75 ten thousand yuan/year, and other obtained technical effects and economic benefits are shown in table 5.
[ example 5 ]
Similarly, in example 1, only the production scale was changed to 100 ten thousand tons/year of ethylene process equipment, and by using the method for recovering pressure energy by using the ethylene plant of the present invention, 64.22% of external energy supply was relatively saved, 95 ten thousand yuan/year of electric power cost was saved, and other obtained technical effects and economic benefits are shown in table 5.
[ example 6 ]
Similarly, in example 1, only the production scale was changed to 150 ten thousand tons/year of ethylene process equipment, and by using the method for recovering pressure energy by using the ethylene plant of the present invention, 65.61% of external energy supply was relatively saved, 143 ten thousand yuan/year of electric power cost was saved, and other technical effects and economic benefits were obtained, as shown in table 5.
[ example 7 ]
As in [ example 5 ], the production scale was still 100 million tons per year of ethylene process plant, with only the process parameters changed as follows: the pyrolysis gas 11 entering the bottom of the absorption tower 1 contains acid gas hydrogen sulfide H2S and carbon dioxide CO2 with the mole fraction of 0.02 percent; the purified cracking gas 12 flowing out of the top of the absorption tower 1 contains acid gas hydrogen sulfide H2S and carbon dioxide CO2 with the mole fraction less than or equal to 2.0 ppm. The operation pressure of the absorption tower 1 is 1.5MPa, the operation temperature of the top of the tower is 55 ℃, and the operation temperature of the bottom of the tower is 58 ℃. The absorption tower 1 adopts monoethanolamine MEA with the mole fraction of 15 percent as an absorbent. The operating pressure of the desorption tower 6 is 0.1MPa, the operating temperature of the top of the tower is 100 ℃, and the operating temperature of the bottom of the tower is 104 ℃. The desorption tower 6 adopts the external supply direct steam to operate at the pressure of 0.2MPa and the operating temperature of 140 ℃. The inlet operating pressure of the pressure reduction end of the pressure recovery device 3 is 1.5MPa, and the outlet operating pressure is 0.4 MPa; the inlet operating pressure of the boosting end is 0.9MPa, and the outlet operating pressure is 1.9 MPa. The preposed booster pump 5 is started, the inlet operation pressure is 0.1MPa, and the outlet operation pressure is 0.9 MPa.
By adopting the method for recovering the pressure energy by the ethylene device, 64.02% of externally supplied energy is relatively saved, 95 ten thousand yuan/year of electric power cost is saved, and other obtained technical effects and economic benefits are shown in Table 5.
[ example 8 ]
As in [ example 5 ], the production scale was still 100 million tons per year of ethylene process plant, with only the process parameters changed as follows: the pyrolysis gas 11 entering the bottom of the absorption tower 1 contains acid gas hydrogen sulfide H2S and carbon dioxide CO2 with the mole fraction of 0.19%; the purified cracking gas 12 flowing out of the top of the absorption tower 1 contains acid gas hydrogen sulfide H2S and carbon dioxide CO2 with the mole fraction less than or equal to 2.0 ppm. The operating pressure of the absorption tower 1 is 2.5MPa, the operating temperature of the top of the tower is 72 ℃, and the operating temperature of the bottom of the tower is 75 ℃. The absorption tower 1 adopts 35 percent of diethanolamine DEA as an absorbent. The operating pressure of the desorption tower 6 is 1.1MPa, the operating temperature of the top of the tower is 115 ℃, and the operating temperature of the bottom of the tower is 119 ℃. The desorption tower 6 adopts the direct steam supplied from the outside to operate at the pressure of 1.2MPa and the operating temperature of 208 ℃. The inlet operating pressure of the pressure reduction end of the pressure recovery device 3 is 2.5MPa, and the outlet operating pressure is 1.4 MPa; the inlet operating pressure of the boosting end is 1.9MPa, and the outlet operating pressure is 2.9 MPa. The preposed booster pump 5 is started, the inlet operation pressure is 1.1MPa, and the outlet operation pressure is 1.9 MPa.
By adopting the method for recovering the pressure energy by the ethylene device, 63.98% of externally supplied energy is relatively saved, 95 ten thousand yuan/year of electric power cost is saved, and other obtained technical effects and economic benefits are shown in Table 5.
In summary, the technical effects and economic benefits obtained by adopting the technical scheme of the ethylene device for recovering pressure energy of the invention are shown in table 5 in the embodiment 1 to the embodiment 8.
TABLE 5 summary of the technical and economic benefits of the invention
Claims (1)
1. A method for recovering pressure energy of an ethylene plant comprises the following steps:
(a) the method comprises the steps that a pyrolysis gas which flows out of an out-of-range ethylene cracking furnace and is quenched and compressed enters the bottom of an absorption tower, meanwhile, a low-temperature barren solution absorbent with reduced temperature and increased pressure enters the top of the absorption tower, the pyrolysis gas is in countercurrent contact with the low-temperature barren solution absorbent in the absorption tower, an acid gas in the pyrolysis gas is absorbed by the low-temperature barren solution absorbent, the purified pyrolysis gas with the acid gas removed flows out of the top of the absorption tower, and meanwhile, a high-pressure rich solution absorbent for absorbing the acid gas is formed;
(b) the high-pressure rich liquid absorbent for absorbing the acid gas flows out of the bottom of the absorption tower and is heated into a high-temperature rich liquid absorbent through heat exchange of the lean rich absorbent heat exchanger; the high-temperature rich liquid absorbent enters a pressure recovery device;
(c) under the normal working condition, the high-temperature rich liquid absorbent enters an inlet of a pressure reduction end of the pressure recovery device, the pressure of the high-temperature rich liquid absorbent is converted from high pressure to low pressure to form a low-pressure rich liquid absorbent, and the low-pressure rich liquid absorbent flowing out of the pressure recovery device enters the top of a desorption tower; the material flow from the bottom of the absorption tower is divided into two paths, one path enters the pressure recovery device, the other path is a bypass pipeline A, a valve is arranged on the bypass pipeline A, the outlet of the bypass pipeline A is connected with the outlet pipeline of the pressure reduction end of the pressure recovery device, and the valve on the bypass pipeline A is closed under the normal working condition;
(d) externally supplied steam enters the bottom of the desorption tower; in the desorption tower, externally supplying steam to reduce the partial pressure of the low-pressure rich liquid absorbent and increase the temperature of the low-pressure rich liquid absorbent, wherein the low-pressure rich liquid absorbent is in countercurrent contact with the externally supplied steam to carry out steam stripping regeneration, acid gas in the low-pressure rich liquid absorbent is desorbed by the externally supplied steam, and the desorbed acid gas flows out of the top of the desorption tower and is conveyed out of the room, so that the low-pressure lean liquid absorbent is formed;
(e) the low-pressure barren solution absorbent for removing the acid gas flows out of the bottom of the desorption tower and is divided into two paths, one path is connected with the inlet of the preposed booster pump, the outlet of the preposed booster pump is connected with the inlet of the boosting end of the pressure recovery device, the other path is a bypass pipeline B, and a standby booster pump is arranged on the bypass pipeline B; under the normal working condition, the inlet valve and the outlet valve of the standby booster pump and the standby booster pump are closed, and the low-pressure barren liquor absorbent from the bottom of the desorption tower enters the inlet of the boosting end of the pressure recovery device after being boosted by the preposed booster pump;
(f) in the pressure recovery device, the pressure energy of the high-temperature rich liquid absorbent at the high-pressure side of the decompression end is converted into mechanical energy of the rotating shaft and then converted into the pressure energy of the low-pressure barren liquid absorbent at the low-pressure side of the boosting end, the pressure of the low-pressure barren liquid absorbent is increased and converted into the high-pressure barren liquid absorbent, and the pressure meets the pressure required by the absorption operation of the absorption tower, so that the output pressure of the preposed booster pump is reduced, and the power consumption of a motor is reduced;
(g) under the normal working condition, the low-pressure barren liquor absorbent from the bottom of the desorption tower enters an inlet at the pressure boosting end of a pressure recovery device, the pressure of the low-pressure barren liquor absorbent is converted from low pressure to high pressure in the pressure recovery device, the high-pressure barren liquor absorbent flowing out of the pressure recovery device returns to the top of the absorption tower after the temperature of the high-pressure barren liquor absorbent is reduced by a barren and rich absorbent heat exchanger to be recycled, and acid gas in the cracked gas is absorbed;
the pressure recovery device is an online pressure recovery device adopting a hydraulic turbine principle, and the device directly connects a pressure reduction end high-pressure side impeller and a pressure boosting end low-pressure side impeller in the same pump body through a rotating shaft, a high-pressure rich liquid absorbent at the pressure reduction end drives the pressure reduction end high-pressure side impeller, and drives the pressure boosting end low-pressure side impeller to rotate through the rotating shaft, so that the pressure of a low-pressure lean liquid absorbent at the pressure boosting end is increased, the pressure energy at the pressure reduction end high-pressure side is converted into mechanical energy of the rotating shaft and then converted into pressure energy at the pressure boosting end low-pressure side, and the rotating shaft in the pressure recovery device is the only operating part, so that the pressure recovery device has no shaft seal and no additional lubricating system; when the pressure recovery device has a fault working condition, simultaneously starting a valve on a pressure bypass pipeline A and a standby booster pump on a bypass pipeline B, enabling a high-temperature rich liquid absorbent to pass through a pipeline A from a lean-rich absorbent heat exchanger to a pressure reduction end outlet pipeline of the pressure recovery device and further to the top of a desorption tower, enabling a low-pressure lean liquid absorbent to pass through the bypass pipeline B and the standby booster pump to be pressurized and then to a pressure boosting end outlet pipeline of the pressure recovery device and further to return to the top of the absorption tower, and starting the operating working condition without using the pressure recovery device, so that the absorbent is ensured to normally circulate between the absorption tower and the desorption tower; the mole fraction of the acid gas contained in the cracking gas entering the bottom of the absorption tower is 0.02-0.19%; the mole fraction of acid gas contained in the purified pyrolysis gas flowing out of the top of the absorption tower is less than or equal to 2.0 ppm; the acid gases are hydrogen sulfide H2S and carbon dioxide CO 2; the operating pressure range of the absorption tower is 1.5-2.5 MPa, the operating temperature range of the tower top is 55-72 ℃, and the operating temperature range of the tower bottom is 58-75 ℃; the absorption tower adopts 15-20% of monoethanolamine MEA or 25-35% of diethanolamine DEA as an absorbent; the operating pressure range of the desorption tower is 0.1-1.1 MPa, the operating temperature range of the top of the tower is 100-115 ℃, and the operating temperature range of the bottom of the tower is 104-119 ℃; the desorption tower adopts externally supplied steam with the operating pressure ranging from 0.2MPa to 1.2MPa and the operating temperature ranging from 140 ℃ to 208 ℃; the inlet operating pressure range of the pressure reduction end of the pressure recovery device is 1.5-2.5 MPa, and the outlet operating pressure range is 0.4-1.4 MPa; the inlet operating pressure range of the boosting end is 0.9-1.9 MPa, and the outlet operating pressure range is 1.9-2.9 MPa; and starting the preposed booster pump, wherein the inlet operating pressure range is 0.1-1.1 MPa, and the outlet operating pressure range is 0.9-1.9 MPa.
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| CN102900477A (en) * | 2011-07-27 | 2013-01-30 | 北京航天动力研究所 | High-power hydraulic turbine energy recovery system |
| CN105026013A (en) * | 2012-11-08 | 2015-11-04 | 能量回收股份有限公司 | Isobaric pressure exchanger in amine gas processing |
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| US9901861B2 (en) * | 2011-10-18 | 2018-02-27 | General Electric Technology Gmbh | Chilled ammonia based CO2 capture system with wash system and processes of use |
| CN103373898B (en) * | 2012-04-20 | 2016-02-24 | 新奥科技发展有限公司 | Methanol synthesizing process, system for methanol synthesis |
| US20160166976A1 (en) * | 2013-07-23 | 2016-06-16 | Prateek Bumb | Split line system, method and process for co2 recovery |
| KR20150017050A (en) * | 2013-08-05 | 2015-02-16 | 재단법인 포항산업과학연구원 | Method for the prevention of ammonia vaporization in carbon dioxide absorption process and apparatus for absorbing carbon dioxide using thereof |
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| CN105026013A (en) * | 2012-11-08 | 2015-11-04 | 能量回收股份有限公司 | Isobaric pressure exchanger in amine gas processing |
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