CN107243242A - Refinery's amine liquid desulphurization system and its sulfur method - Google Patents
Refinery's amine liquid desulphurization system and its sulfur method Download PDFInfo
- Publication number
- CN107243242A CN107243242A CN201710367441.9A CN201710367441A CN107243242A CN 107243242 A CN107243242 A CN 107243242A CN 201710367441 A CN201710367441 A CN 201710367441A CN 107243242 A CN107243242 A CN 107243242A
- Authority
- CN
- China
- Prior art keywords
- refinery
- tower
- regeneration
- desulfurizing tower
- refinery gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Analytical Chemistry (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of refinery's amine liquid desulphurization system, including the first refinery gas desulfurizing tower, second refinery gas desulfurizing tower, rich solution flash tank and solvent regeneration tower, the bottom inlet of first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower is respectively used to be passed through catalysis drying gas and catalytic liquefaction gas, the tower reactor of first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower is connected to flash rich solution by pipeline with the entrance of rich solution flash tank, the outlet of rich solution flash tank is connected by the entrance of pipeline and solvent regeneration tower, first regeneration lean solution outlet of solvent regeneration tower is connected by pipeline with the desulfurizing agent entrance of the first refinery gas desulfurizing tower, second regeneration lean solution outlet of solvent regeneration tower is connected by pipeline with the desulfurizing agent entrance of the second refinery gas desulfurizing tower, regeneration depth of the regeneration depth of second regeneration lean solution outlet higher than the first regeneration lean solution outlet.Refinery's amine liquid desulphurization system proposed by the present invention and its sulfur method, reduce the load of regenerator, improve its regeneration efficiency.
Description
Technical field
The present invention relates to oil refining technical field, more particularly to a kind of refinery's amine liquid desulphurization system and its sulfur method.
Background technology
In refinery production process, feedstock oil passes through part sulfide in primary and secondary processing, feedstock oil and is converted into
H2S, H2S is entered eventually into the products such as dry gas, gasoline, liquefied petroleum gas.If these sulfur-bearing product desulfurization are not up to standard, as
Petrochemical materials or fuel will cause equipment, the corrosion of pipeline when using, ultimately cause environmental pollution, and then harmful to human
Health.In recent years, with the development of national economy, oil demand amount is increasing so that domestic refinery is to sour crude and bad
The processing capacity of matter crude oil constantly increases, and the substantial amounts of sulfur-bearing product of by-product, adds the load of desulfurization in production.On the other hand,
To reduce pollution of the discharge to environment, country is also more and more stricter to the quality requirement of fuel product.
Conventional desulfurizing agent is usually a kind of reproducible aqueous absorbent, at present, the flowage structure of refinery's amine liquid desulfurization
It can be generally divided into two classes：One class is to absorb desulfurization to be partially dispersed in each corollary apparatus, and solvent reclamation is divided in each device
Dissipate regeneration.Another kind of is to absorb desulfurization to be partially dispersed in each corollary apparatus, and rich solvent is focused in same regenerator and concentrated
Regeneration.Although rich solvent, which is focused in same regenerator, concentrates regeneration method to reduce equipment investment cost, then
The load of raw tower is too big, makes its service life reduction, is also easy to be contaminated amine liquid in addition, once there is such as band oil in amine liquid system
The problems such as band hydrocarbon, amine liquid foam is searched extremely difficult.
The content of the invention
It is a primary object of the present invention to provide a kind of refinery's amine liquid desulphurization system and its sulfur method, it is intended to reduction regeneration
The load of tower, while improving its regeneration efficiency.
To achieve the above object, the present invention provides a kind of refinery's amine liquid desulphurization system, including the first refinery gas desulfurizing tower, the
Two refinery gas desulfurizing towers, rich solution flash tank and solvent regeneration tower, wherein,
The bottom inlet of the first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower is respectively used to be passed through catalysis drying gas and urged
The tower reactor of change liquefied gas, the first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower passes through pipeline and rich solution flash tank
Entrance is connected to be flashed to rich solution, and the outlet of the rich solution flash tank is connected by the entrance of pipeline and solvent regeneration tower,
First regeneration lean solution outlet of the solvent regeneration tower is connected by pipeline with the desulfurizing agent entrance of the first refinery gas desulfurizing tower, institute
The the second regeneration lean solution outlet for stating solvent regeneration tower is connected by pipeline with the desulfurizing agent entrance of the second refinery gas desulfurizing tower, described
Regeneration depth of the regeneration depth of second regeneration lean solution outlet higher than the first regeneration lean solution outlet.
Preferably, the regenerator for being boosted to rich solution is also equipped with the pipeline in the rich solution flash tank exit
Feed pump, rich solution is boosted after rich solution flash tank flash distillation removing part lighter hydrocarbons by regenerator feed pump, and the rich solution flash tank enters
The rich solution blender for being mixed to rich solution is also equipped with pipeline at mouthful.
Preferably, refinery's amine liquid desulphurization system also includes being provided with First Heat Exchanger, the First Heat Exchanger mutually
The first flow and second flow channel of heat exchange, the entrance of First Heat Exchanger first flow are connected with the outlet of rich solution flash tank, and first changes
The outlet of hot device first flow and the entrance of solvent regeneration tower are connected, First Heat Exchanger second flow channel entrance and the first regeneration lean solution
Outlet connection, First Heat Exchanger second flow channel outlet is connected with the desulfurizing agent entrance of the first refinery gas desulfurizing tower.
Preferably, refinery's amine liquid desulphurization system also includes being provided with the second heat exchanger, second heat exchanger mutually
The first flow and second flow channel of heat exchange, the entrance of the second heat exchanger first flow are connected with First Heat Exchanger, the second heat exchanger
The outlet of first flow and the entrance of solvent regeneration tower are connected, the second heat exchanger second flow channel entrance and the second regeneration lean solution outlet
Connection, the second heat exchanger second flow channel outlet is connected with the desulfurizing agent entrance of the second refinery gas desulfurizing tower.
Preferably, it is also equipped with the first cooler on the pipeline in the second heat exchanger second flow channel exit.
Preferably, the solvent regeneration tower bottom of towe is additionally provided with the reboiler that bottom temperature is taken for maintenance.
Preferably, refinery's amine liquid desulphurization system also includes the second cooler and acid being sequentially connected with solvent regeneration tower
Property qi leel flow container, acid water that acid qi leel flow container is isolated returns to solvent regeneration tower top and flows back, and acid qi leel flow container divides
The sour gas separated out delivers to sulfur recovery facility.
Present invention further propose that a kind of sulfur method based on above-mentioned refinery's amine liquid desulphurization system, Bao includes Yi Xia Walk
Suddenly：
Catalysis drying gas enters the first refinery gas desulfurizing tower bottom, with the reproducible desulfurization come from the first refinery gas desulfurizing tower top
Agent counter current contacting, is purified the first refinery gas logistics and high H2The rich solution of S loads, while catalytic liquefaction gas enters the second refinery
Desulfurization tower bottom, the reproducible desulfurizing agent counter current contacting with coming from the second refinery gas desulfurizing tower top, is purified second
Refinery gas logistics and low H2The rich solution of S loads；
Enter after being deaerated after the tower reactor rich solution mixing of first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower through rich solution flash tank
Solvent regeneration tower, the lean solution of the regeneration lean solution outlet outflow of solvent regeneration tower first delivers to the first refinery gas desulfurizing tower as desulfurizing agent
Recycle, the lean solution of the regeneration lean solution outlet outflow of solvent regeneration tower second is delivered to the second refinery gas desulfurizing tower and followed as desulfurizing agent
Ring is used.
Preferably, the feeding temperature for controlling catalysis drying gas to enter the first refinery gas desulfurizing tower is 15 DEG C ~ 50 DEG C, control catalysis
The feeding temperature that liquefied gas enters the second refinery gas desulfurizing tower is 15 DEG C ~ 50 DEG C, the first refinery gas desulfurizing tower and the second refinery gas
The operation temperature of desulfurizing tower is 20 DEG C ~ 65 DEG C, and the operating pressure of the first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower is
0.1MPa~10MPa。
Preferably, by being boosted through regenerator feed pump after rich solution deaerates through flash tank, pressure is 0.1MPa ~ 6MPa, boosting
Temperature control is 75 DEG C ~ 115 DEG C after rich solution afterwards exchanges heat through First Heat Exchanger；Solvent regeneration tower column bottom temperature maintain 90 DEG C ~
150℃。
Amine liquid desulphurization system in refinery's proposed by the present invention, is divided into two lines output, so by solvent again by solvent regeneration tower
Raw tower is divided into upper and lower two parts, and the lean solution of upper part is regenerated using low depth, and lower part lean solution is using complete regeneration, by subtracting
This method of regeneration depth of small lean solution reduces the purpose of reboiler to reach.Meanwhile, carried out using rich solution flash tank high
Warm low pressure flash, reduces regenerated acidic gas hydrocarbon content, reduces the waste of efficient resource.In addition, by same H2The richness of S loads
Absorbent carries out concentration regeneration, and its regeneration efficiency is high, while reducing equipment investment.
Brief description of the drawings
Fig. 1 is the structural representation of amine liquid desulphurization system in refinery's of the present invention.
In figure, C101- the first refinery gas desulfurizing towers, C102- the second refinery gas desulfurizing towers, C103- solvent regeneration towers,
D101- removes flow container, D102- rich solution blenders, D103- rich solution flash tanks, D104- acidity qi leel flow containers, D105- solvent tanks,
D106- condensers, the heat exchangers of E101- second, the coolers of E102- first, the coolers of E103- second, E104- reboilers, E105-
First Heat Exchanger, P101- regenerator feed pumps, P102- acid solution reflux pumps, the feed pumps of P103- second, the feed pumps of P104- first.
The realization, functional characteristics and advantage of the object of the invention will be described further referring to the drawings in conjunction with the embodiments.
Embodiment
It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, it is not used to limit this hair
It is bright.
It should be noted that in the description of the invention, term " transverse direction ", " longitudinal direction ", " on ", " under ", "front", "rear",
The orientation or position relationship of the instruction such as "left", "right", " vertical ", " level ", " top ", " bottom ", " interior ", " outer " is based on accompanying drawing institutes
The orientation or position relationship shown, is for only for ease of the description present invention and simplifies description, is not instruction or implies signified dress
Put or element there must be specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to the limit of the present invention
System.In addition, term " first ", " second " etc. are only used for describing purpose, and it is not intended that indicating or implying relative importance.
The present invention proposes a kind of refinery's amine liquid desulphurization system.
In reference picture 1, this preferred embodiment, a kind of refinery's amine liquid desulphurization system, including the first refinery gas desulfurizing tower C101,
Second refinery gas desulfurizing tower C102, rich solution flash tank D103 and solvent regeneration tower C103, wherein,
First refinery gas desulfurizing tower C101 and the second refinery gas desulfurizing tower C102 bottom inlet are respectively used to be passed through catalysis drying gas
With catalytic liquefaction gas, the first refinery gas desulfurizing tower C101 and the second refinery gas desulfurizing tower C102 tower reactor pass through pipeline and rich solution
Flash tank D103 entrance is connected to be flashed to rich solution, and rich solution flash tank D103 outlet passes through pipeline and solvent regeneration tower
C103 entrance connection, solvent regeneration tower C103 the first regeneration lean solution outlet passes through pipeline and the first refinery gas desulfurizing tower C101
Desulfurizing agent entrance connection, solvent regeneration tower C103 second regeneration lean solution outlet pass through pipeline and the second refinery gas desulfurizing tower
C102 desulfurizing agent entrance connection, the regeneration depth of the second regeneration lean solution outlet is deep higher than the regeneration of the first regeneration lean solution outlet
Degree.
It is additionally provided with first refinery gas desulfurizing tower C101 bottom inlet except flow container D101.Catalysis drying gas enters the first refinery
The optional position of desulfurization tower C101 bottoms.Catalytic liquefaction gas enters the optional position of the second refinery gas desulfurizing tower C102 bottoms.
First refinery gas desulfurizing tower C101 and the second refinery gas desulfurizing tower C102 desulfurizing agent entrance are arranged on the optional position in portion.
First is separately installed with first refinery gas desulfurizing tower C101 and the second refinery gas desulfurizing tower C102 desulfurizing agent porch pipeline
Feed pump P104 and the second feed pump P103.Desulfurizing agent in first refinery gas desulfurizing tower C101 and the second refinery gas desulfurizing tower C102
For the aqueous mixture containing weak base, as needed, other components can be also added wherein, weak base can be alkanolamine, for example
MEA, diethanol amine, methyl diethanolamine etc..Desulfurizing agent usually contains 10% ~ 50%（Mass fraction）Alkaline constituents, 10% ~
90%（Mass fraction）Water and 0 ~ 50%（Mass fraction）Other components.First refinery gas desulfurizing tower C101, the second refinery gas
Desulfurizing tower C102 and solvent regeneration tower C103 can be any effective mass transfer tower structures, for example packed tower, bubble column,
Sieve-plate tower, valve tower etc..Pump is using energy-saving chemical flow-process pump in this refinery's amine liquid desulphurization system and is equipped with energy-saving electrical machine,
Improve the efficiency of pump and motor.
Further, the regeneration for being boosted to rich solution is also equipped with the pipeline in rich solution flash tank D103 exits
Tower feed pump P101, rich solution is boosted after rich solution flash tank D103 flash distillation removing part lighter hydrocarbons by regenerator feed pump P101, rich
The rich solution blender D102 for being mixed to rich solution is also equipped with the pipeline of liquid flash tank D103 porch.
Further, this refinery's amine liquid desulphurization system also includes setting on First Heat Exchanger E105, First Heat Exchanger E105
It is equipped with the first flow exchanged heat mutually and second flow channel, entrance and the rich solution flash tank D103 of First Heat Exchanger E105 first flows
Outlet connection, the outlet of First Heat Exchanger E105 first flows is connected with solvent regeneration tower C103 entrance, First Heat Exchanger
E105 second flow channels entrance is connected with the first regeneration lean solution outlet, the outlet of First Heat Exchanger E105 second flow channels and the first refinery gas
Desulfurizing tower C101 desulfurizing agent entrance connection.
Further, this refinery's amine liquid desulphurization system also includes setting on the second heat exchanger E101, second heat exchanger E101
It is equipped with the first flow exchanged heat mutually and second flow channel, entrance and the First Heat Exchanger E105 of the second heat exchanger E101 first flows
Connection, the outlet of the second heat exchanger E101 first flows is connected with solvent regeneration tower C103 entrance, the second heat exchanger E101 the
Two flow channel entry points are connected with the second regeneration lean solution outlet, the outlet of the second heat exchanger E101 second flow channels and the second refinery gas desulfurizing tower
C102 desulfurizing agent entrance connection.By First Heat Exchanger E105 and the second heat exchanger E101 formation heat-exchange networks, so that effectively
Ground reduces energy consumption.
The first cooler device E102 is also equipped with the pipeline in the second heat exchanger E101 second flow channels exit.Second charging
Solvent tank D105 is also equipped between pump P103 and the first cooler device E102.
Further, solvent regeneration tower C103 bottom of towe is additionally provided with the reboiler E104 that bottom temperature is taken for maintenance.Reboiler
E104 thermal source is by steam（Steam is arranged on 0.4MPa）There is provided, to prevent reboiler tube bank wall temperature too high, so as to cause solvent
Thermal degradation.In addition, reboiler E104 uses low-pressure steam as thermal source, existing thermal source and low-temperature receiver are made full use of, energy consumption is small.
Further, this refinery's amine liquid desulphurization system also includes the second cooler being sequentially connected with solvent regeneration tower C103
E103 and acid qi leel flow container D104, the acid water that acid qi leel flow container D104 is isolated returns to solvent regeneration tower C103 tops and made
Backflow, the sour gas that acid qi leel flow container D104 is isolated delivers to sulfur recovery facility.
Amine liquid desulphurization system in refinery's proposed by the present invention, by solvent regeneration tower, C103 points are two lines output, so will be molten
C103 points of agent regenerator is upper and lower two parts, and the lean solution of upper part is regenerated using low depth, and lower part lean solution is using completely again
It is raw, the purpose of reduction reboiler E104 loads is reached by reducing this method of regeneration depth of lean solution.Meanwhile, utilize rich solution
Flash tank D103 carries out high-temperature low-pressure flash distillation, reduces regenerated acidic gas hydrocarbon content, reduces the waste of efficient resource.In addition, passing through
To same H2The rich absorbent of S loads carries out concentration regeneration, and its regeneration efficiency is high, while reducing equipment investment.
Present invention further propose that a kind of sulfur method of refinery's amine liquid desulphurization system.
A kind of sulfur method based on above-mentioned refinery's amine liquid desulphurization system, it is rapid that Bao includes Yi Xia Walk：
Catalysis drying gas enter the first refinery gas desulfurizing tower C101 bottoms, with from the first refinery gas desulfurizing tower C101 tops come can be again
Raw desulfurizing agent counter current contacting, is purified the first refinery gas logistics and high H2The rich solution of S loads, while catalytic liquefaction gas enters
Second refinery gas desulfurizing tower C102 bottoms, with being connect from the next reproducible desulfurizing agent adverse current in the second refinery gas desulfurizing tower C102 tops
Touch, be purified the second refinery gas logistics and low H2The rich solution of S loads；
Through rich solution flash tank after first refinery gas desulfurizing tower C101 and the second refinery gas desulfurizing tower C102 tower reactor rich solution mixing
Enter solvent regeneration tower C103 after D103 degassings, the lean solution of the regeneration lean solution outlet outflows of solvent regeneration tower C103 first delivers to first
Refinery gas desulfurizing tower C101 is recycled as desulfurizing agent, and the lean solution of the regeneration lean solution outlet outflows of solvent regeneration tower C103 second is sent
Recycled to the second refinery gas desulfurizing tower C102 as desulfurizing agent.
Specifically, the feeding temperature for controlling catalysis drying gas to enter the first refinery gas desulfurizing tower C101 is 15 DEG C ~ 50 DEG C, control
The feeding temperature that catalytic liquefaction gas enters the second refinery gas desulfurizing tower C102 is 15 DEG C ~ 50 DEG C（It is preferred that 33 DEG C）, the first refinery gas
Desulfurizing tower C101 and the second refinery gas desulfurizing tower C102 operation temperature are 20 DEG C ~ 65 DEG C（It is preferred that 30 DEG C）, the first refinery gas
Desulfurizing tower C101 and the second refinery gas desulfurizing tower C102 operating pressure are 0.1MPa ~ 10MPa（It is preferred that 1.2 MPa）.At these
Under the conditions of, sulfur content in first and second refinery gas being purified can be made to reach emission request.
Specifically, by being boosted through regenerator feed pump P101 after rich solution deaerates through flash tank, pressure is 0.1MPa ~ 6MPa,
Temperature control is 75 DEG C ~ 115 DEG C after rich solution after boosting exchanges heat through First Heat Exchanger E105；Solvent regeneration tower C103 column bottom temperatures
Maintain 90 DEG C ~ 150 DEG C.Under these conditions, reboiler heat duty can be reduced, regenerated acidic gas hydrocarbon content is reduced, reduced
The waste of efficient resource.
The present invention herein proposes following embodiment.
Embodiment 1
Sulfur removal technology process is as follows：With 4900m3/ h inlet amount, 38 DEG C of feeding temperature, 1.0MPa feed pressure are by dry gas
The first refinery gas desulfurizing tower C101 bottoms are sent into, the operation temperature of tower is 36 DEG C, and operating pressure is 0.85MPa, solvent regeneration tower
The low depth absorbent regeneration N methyldiethanol amine of C103 side take-offs（MDEA）Send on the first refinery gas desulfurizing tower C101
Portion, both counter current contactings carry out mass transfer.Acidic materials in dry gas（H2S、CO2）Absorbed etc. agent is desulfurized, the dry gas being purified
Logistics（H2S=10mg/m3≤150mg/m3）With high H2The rich solution of S loads.
Liquefied gas feeding second is refined with 30000kg/h inlet amount, 35 DEG C of feeding temperature, 1.3MPa feed pressure
Factory desulfurization tower C102 bottoms, the operation temperature of tower is 35 DEG C, and operating pressure is 1.112MPa, make its with from solvent regeneration tower
The concentration that C103 bottoms regenerate completely is 30wt% absorbent MDEA（N methyldiethanol amine）Counter current contacting, after fully absorbing
The liquefied gas logistics being purified（H2S=5mg/m3≤50mg/m3）With low H2The rich solution of S loads.
Low H2The rich solution of S loads and high H2The rich solution of S loads mixed in blending tank after to First Heat Exchanger E105 exchange heat to
Enter rich solution flash tank D103 after 90 DEG C, boosting to 0.31MPa by regenerator feed pump P101 after flash liberation enters solvent
Regenerator C103 regenerates, and solvent regeneration tower C103 operation temperature is 100 DEG C, and operating pressure is 0.06MPa, solvent regeneration tower
C103 bottom of towe is provided with reboiler, maintains 115 DEG C of column bottom temperature, and the deep regenerative lean solution that solvent regeneration tower C103 bottoms come out delivers to the
Two heat exchanger E101 heat exchange, which is cooled to after 38 DEG C, enters solvent tank D105, and the second refinery gas desulfurizing tower C102 conducts are sent into afterwards
Desulfurizing agent is recycled.The sour gas that solvent regeneration tower C103 tower tops come out enters regenerated acid after being cooled down through the second cooler E103
Property qi leel flow container D104 carry out gas-liquid separation after deliver to sulfur recovery facility, the liquid phase of regenerated acidic qi leel flow container D104 bottoms is returned
Solvent regeneration tower C103 upper returns are returned to recycle.Solvent regeneration tower C103 side take-offs necessarily regenerate the rich solution of depth through changing
The first refinery gas desulfurizing tower C101 tops are squeezed into by booster after the cooling of hot device it is used as desulfurizing agent and recycles.The absorption of loss
Agent is by poor dose of external supplement of device.
Embodiment 2
Other each steps are same as Example 1 except operating parameter for the present embodiment sulfur removal technology, and design parameter is as follows：Absorbent
Concentration 45wt%, liquefied gas inlet amount 30000kg/h, 30 DEG C of feeding temperature, feed pressure 1.1MPa, the behaviour of desulfuration of liquefied gas tower
Make 35 DEG C of temperature, operating pressure 1MPa, dry gas inlet amount 4900m3/ h, 30 DEG C of feeding temperature, feed pressure 0.9MPa, the first refining
35 DEG C of factory's desulfurization tower C101 operation temperatures, operating pressure 0.8MPa, the second 80 DEG C of heat exchanger E101 temperature, regenerator feed pump
P101 boosts to 0.1MPa, and 90 DEG C of solvent regeneration tower C103 operation temperatures, operating pressure 0.03MPa, reboiler maintains bottom of towe temperature
110 DEG C of degree, the second heat exchanger E101 30 DEG C of chilling temperatures of heat exchange.
Embodiment 3
Other each steps are same as Example 1 except operating parameter for the present embodiment sulfur removal technology, and design parameter is as follows：Absorbent
The wt% of concentration 15, liquefied gas inlet amount 30000kg/h, 40 DEG C of feeding temperature, feed pressure 2.1MPa, the behaviour of desulfuration of liquefied gas tower
Make temperature 45 C, the MPa of operating pressure 2, dry gas inlet amount 4900m3/ h, 40 DEG C of feeding temperature, feed pressure 1.1MPa, first
45 DEG C of refinery gas desulfurizing tower C101 operation temperature, operating pressure 1MPa, the second 110 DEG C of heat exchanger E101 temperature, regenerator enters
Material pump P101 boosts to 0.3MPa, and 110 DEG C of solvent regeneration tower C103 operation temperatures, operating pressure 0.1MPa, reboiler maintains tower
130 DEG C of bottom temperature, the second 50 DEG C of chilling temperature of heat exchange.
Embodiment 4
Other each steps are same as Example 1 except operating parameter for the present embodiment sulfur removal technology, and design parameter is as follows：Using suction
The wt% of agent concentration 32 is received, the feeding temperature that liquefied gas enters desulfuration of liquefied gas tower is 33 DEG C, liquefied gas inlet amount 30000kg/h,
Feed pressure 1.3MPa, 32 DEG C of the operation temperature of desulfuration of liquefied gas tower, operating pressure is 1.2MPa, is purified after fully absorbing
Liquefied gas logistics（H2S=2mg/m3≤50mg/m3）, the feeding temperature that dry gas enters the first refinery gas desulfurizing tower C101 is 35
DEG C, dry gas inlet amount is 4900m3/ h, the first refinery gas desulfurizing tower C101 operation temperature are 38 DEG C, and operating pressure is
0.9MPa, is fully absorbed after desulfurization, the dry gas logistics being purified（H2S=3mg/m3≤150mg/m3）In second heat exchanger E101
Heat-exchange temperature be 90 DEG C, regenerator feed pump P101 by rich solution boost to after 0.3MPa enter solvent regeneration tower C103（, reboiling
Device maintains column bottom temperature to be 120 DEG C.
Embodiment 5
Product-the dry gas and liquefied gas of catalytic cracking unit from certain petroleum chemical enterprise, carry out depriving hydrogen sulphide and refine, wherein dry
Gas contains 0.25wt%H2S and 0.54wt%CO2, liquefied gas contains 0.27 wt %H2S.Matter of the petroleum chemical enterprise to product after desulfurization
Measuring requirement is：Purify H in dry gas2S≤150mg/m3, purify H in liquefied gas2S≤50mg/m3。
Desulfurization is carried out using the sulfur method of the present invention, operating condition is：Absorbent is 30wt% N methyldiethanol amine
（MDEA）The aqueous solution, liquefied gas inlet amount is 24388kg/h, 32 DEG C of feeding temperature, feed pressure 1.4MPa, operation temperature 32
DEG C, operating pressure 1.213MPa；Dry gas inlet amount is 4366m3/ h, 38 DEG C of feeding temperature, feed pressure 1.0MPa, operation temperature
30 DEG C, operating pressure 0.95MPa；Second 90 DEG C of heat exchanger E101 temperature, boost pressure 0.26MPa, solvent regeneration tower C103 behaviour
Make 105 DEG C of temperature, operating pressure 0.1MPa, reboiler maintains 123 DEG C of column bottom temperature, exchange heat 38 DEG C of chilling temperature.
In order to be contrasted, we by same dry gas and liquefied gas under the same operating conditions（With previous embodiment 5
Condition is identical）Desulfurization is carried out respectively, and the rich solution after desulfurization is concentrating regeneration after merging, now lean solution needed for the desulfurization of dry gas desulfurizing tower
Measure as 15000kg/h, poor liquid measure needed for desulfuration of liquefied gas tower desulfurization is 3000kg/h, and the amount of regeneration of absorbent is after merging
18000kg/h.And use the inventive method（Fully use suitable regeneration depth）, can be avoided unnecessary reboiler
E104 loads, so as to reduce regenerator reboiler E104 load, solvent regeneration tower C103 reboiler E104 load is by dividing
2602MJ/h before level use is reduced to 2028MJ/h, and 22.06% energy consumption is reduced than before.
The preferred embodiments of the present invention are these are only, are not intended to limit the scope of the invention, it is every to utilize this hair
The equivalent structure transformation that bright specification and accompanying drawing content are made, or other related technical fields are directly or indirectly used in,
Similarly it is included within the scope of the present invention.
Claims (10)
1. a kind of refinery's amine liquid desulphurization system, it is characterised in that including the first refinery gas desulfurizing tower, the second refinery gas desulfurizing tower,
Rich solution flash tank and solvent regeneration tower, wherein,
The bottom inlet of the first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower is respectively used to be passed through catalysis drying gas and urged
The tower reactor of change liquefied gas, the first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower passes through pipeline and rich solution flash tank
Entrance is connected to be flashed to rich solution, and the outlet of the rich solution flash tank is connected by the entrance of pipeline and solvent regeneration tower,
First regeneration lean solution outlet of the solvent regeneration tower is connected by pipeline with the desulfurizing agent entrance of the first refinery gas desulfurizing tower, institute
The the second regeneration lean solution outlet for stating solvent regeneration tower is connected by pipeline with the desulfurizing agent entrance of the second refinery gas desulfurizing tower, described
Regeneration depth of the regeneration depth of second regeneration lean solution outlet higher than the first regeneration lean solution outlet.
2. amine liquid desulphurization system in refinery's as claimed in claim 1, it is characterised in that the pipeline in the rich solution flash tank exit
On be also equipped with regenerator feed pump for being boosted to rich solution, rich solution is after rich solution flash tank flash distillation removing part lighter hydrocarbons
Boosted by regenerator feed pump, the richness for being mixed to rich solution is also equipped with the pipeline of the rich solution flash tank porch
Liquid mixer.
3. amine liquid desulphurization system in refinery's as claimed in claim 1, it is characterised in that also including First Heat Exchanger, this first is changed
The first flow exchanged heat mutually and second flow channel, entrance and the rich solution flash tank of First Heat Exchanger first flow are provided with hot device
Outlet connection, the outlet of First Heat Exchanger first flow and the entrance of solvent regeneration tower are connected, and First Heat Exchanger second flow channel enters
Mouth is connected with the first regeneration lean solution outlet, the outlet of First Heat Exchanger second flow channel and the desulfurizing agent entrance of the first refinery gas desulfurizing tower
Connection.
4. amine liquid desulphurization system in refinery's as claimed in claim 3, it is characterised in that also including the second heat exchanger, this second is changed
The first flow exchanged heat mutually and second flow channel, the entrance and First Heat Exchanger of the second heat exchanger first flow are provided with hot device
The entrance of connection, the outlet of the second heat exchanger first flow and solvent regeneration tower is connected, the second heat exchanger second flow channel entrance with
Second regeneration lean solution outlet connection, the outlet of the second heat exchanger second flow channel and the desulfurizing agent entrance of the second refinery gas desulfurizing tower connect
Connect.
5. amine liquid desulphurization system in refinery's as claimed in claim 4, it is characterised in that the second heat exchanger second flow channel outlet
The first cooler is also equipped with the pipeline at place.
6. amine liquid desulphurization system in refinery's as claimed in claim 1, it is characterised in that the solvent regeneration tower bottom of towe is additionally provided with use
The reboiler of bottom temperature is taken in maintenance.
7. amine liquid desulphurization system in refinery's as claimed in claim 1, it is characterised in that also including being sequentially connected with solvent regeneration tower
The second cooler and acid qi leel flow container, the acid water that acid qi leel flow container is isolated returns to solvent regeneration tower top and returns
Stream, the sour gas that acid qi leel flow container is isolated delivers to sulfur recovery facility.
8. a kind of sulfur method of refinery's amine liquid desulphurization system based on described in claim 3, it is characterised in that Bao includes Yi Xia Walk
Suddenly：
Catalysis drying gas enters the first refinery gas desulfurizing tower bottom, with the reproducible desulfurization come from the first refinery gas desulfurizing tower top
Agent counter current contacting, is purified the first refinery gas logistics and high H2The rich solution of S loads, while catalytic liquefaction gas enters the second refinery
Desulfurization tower bottom, the reproducible desulfurizing agent counter current contacting with coming from the second refinery gas desulfurizing tower top, is purified second
Refinery gas logistics and low H2The rich solution of S loads；
Enter after being deaerated after the tower reactor rich solution mixing of first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower through rich solution flash tank
Solvent regeneration tower, the lean solution of the regeneration lean solution outlet outflow of solvent regeneration tower first delivers to the first refinery gas desulfurizing tower as desulfurizing agent
Recycle, the lean solution of the regeneration lean solution outlet outflow of solvent regeneration tower second is delivered to the second refinery gas desulfurizing tower and followed as desulfurizing agent
Ring is used.
9. the sulfur method of amine liquid desulphurization system in refinery's as claimed in claim 8, it is characterised in that control catalysis drying gas enters
The feeding temperature of first refinery gas desulfurizing tower is 15 DEG C ~ 50 DEG C, and control catalytic liquefaction gas enters entering for the second refinery gas desulfurizing tower
Material temperature degree is 15 DEG C ~ 50 DEG C, and the operation temperature of the first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower is 20 DEG C ~ 65 DEG C,
The operating pressure of first refinery gas desulfurizing tower and the second refinery gas desulfurizing tower is 0.1MPa ~ 10MPa.
10. the sulfur method of amine liquid desulphurization system in refinery's as claimed in claim 8, it is characterised in that rich solution is de- through flash tank
By being boosted through regenerator feed pump after gas, pressure is 0.1MPa ~ 6MPa, temperature after the rich solution after boosting exchanges heat through First Heat Exchanger
Control as 75 DEG C ~ 115 DEG C；Solvent regeneration tower column bottom temperature maintains 90 DEG C ~ 150 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710367441.9A CN107243242A (en) | 2017-05-23 | 2017-05-23 | Refinery's amine liquid desulphurization system and its sulfur method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710367441.9A CN107243242A (en) | 2017-05-23 | 2017-05-23 | Refinery's amine liquid desulphurization system and its sulfur method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107243242A true CN107243242A (en) | 2017-10-13 |
Family
ID=60016814
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710367441.9A Pending CN107243242A (en) | 2017-05-23 | 2017-05-23 | Refinery's amine liquid desulphurization system and its sulfur method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107243242A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108048147A (en) * | 2018-01-26 | 2018-05-18 | 中海石油气电集团有限责任公司 | A kind of amine liquid regenerative system and technique applied to Floating Liquefied Natural Gas facility |
| CN109355121A (en) * | 2018-12-19 | 2019-02-19 | 南京泰斯普化工工程技术有限公司 | A kind of high-efficiency desulfurization system of liquefied gas and device in Gas |
| CN110449007A (en) * | 2018-05-08 | 2019-11-15 | 中国石油化工股份有限公司 | A kind of refinery's amine liquid system optimization utilizes method and device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104307341A (en) * | 2014-11-06 | 2015-01-28 | 上海齐耀螺杆机械有限公司 | Flare gas compression and desulphurization technology |
| CN105013296A (en) * | 2015-08-10 | 2015-11-04 | 中国石油集团工程设计有限责任公司 | Natural gas desulfuration and decarbonization system and method coupling acid gas concentration |
-
2017
- 2017-05-23 CN CN201710367441.9A patent/CN107243242A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104307341A (en) * | 2014-11-06 | 2015-01-28 | 上海齐耀螺杆机械有限公司 | Flare gas compression and desulphurization technology |
| CN105013296A (en) * | 2015-08-10 | 2015-11-04 | 中国石油集团工程设计有限责任公司 | Natural gas desulfuration and decarbonization system and method coupling acid gas concentration |
Non-Patent Citations (2)
| Title |
|---|
| 孙珊珊等: "炼厂胺液脱硫系统多目标优化", 《计算机与应用化学》 * |
| 王正权等: "MDEA吸收法天然气脱硫过程节能途径探讨", 《天然气技术》 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108048147A (en) * | 2018-01-26 | 2018-05-18 | 中海石油气电集团有限责任公司 | A kind of amine liquid regenerative system and technique applied to Floating Liquefied Natural Gas facility |
| CN108048147B (en) * | 2018-01-26 | 2023-11-21 | 中海石油气电集团有限责任公司 | Amine liquid regeneration system and process applied to floating liquefied natural gas facility |
| CN110449007A (en) * | 2018-05-08 | 2019-11-15 | 中国石油化工股份有限公司 | A kind of refinery's amine liquid system optimization utilizes method and device |
| CN110449007B (en) * | 2018-05-08 | 2021-11-09 | 中国石油化工股份有限公司 | Method and device for optimally utilizing refinery amine liquid system |
| CN109355121A (en) * | 2018-12-19 | 2019-02-19 | 南京泰斯普化工工程技术有限公司 | A kind of high-efficiency desulfurization system of liquefied gas and device in Gas |
| CN109355121B (en) * | 2018-12-19 | 2024-05-14 | 南京泰斯普化工工程技术有限公司 | Efficient desulfurization system for liquefied gas and gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104704086B (en) | The method repacking conventional mineral oil refining plant into biorefinery device | |
| CN100473715C (en) | Process flow for raw material pretreatment portion of catalytic dry gas produced phenylethane | |
| CN105693452B (en) | A kind of cleaning system and method for natural gas acetylene | |
| CN101912718B (en) | Device and method for absorbing carbon disulfide in hydrogen sulfide gas by using solvent | |
| CN104892340A (en) | Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption | |
| CN104945224A (en) | Methanol production process | |
| CN104208983B (en) | The decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust | |
| CN107243242A (en) | Refinery's amine liquid desulphurization system and its sulfur method | |
| CN105294394A (en) | Methanol co-production recycling system | |
| CN104138709B (en) | Carbon dioxide recovery system, in accordance and method of operation thereof | |
| CN206924623U (en) | A kind of desulfurization regeneration tower circulates heat riser | |
| CN102489120B (en) | Low temperature methanol wash method and equipment | |
| CN104226096B (en) | Multi-flow-path circulating desulfurization system and multi-flow-path circulating desulfurization method | |
| CN201558655U (en) | System for recovering and treating hydrocarbon-containing waste gas | |
| CN103695043B (en) | Method for drying, purifying and cooling conversion rough synthesized gas and SNG product gas through low-temperature methanol washing and device thereof | |
| CN202355997U (en) | CO2 absorption tower and low-temperature methanol washing equipment comprising same | |
| CN109929638A (en) | A kind of method and apparatus for integrating hydrate and combining acid gas in removing natural gas with hydramine method | |
| CN105833680A (en) | Amine desulphurization method for refinery plant | |
| CN103638802A (en) | Device and method for processing acid gas of refinery plant | |
| WO2010045769A1 (en) | Method and device for short-flow desulfurizing recyled hydrogen | |
| CN103865567B (en) | Desulphurization of recycle hydrogen system and method | |
| CN105169879A (en) | Coked tail gas processing method | |
| CN104667709B (en) | Natural gas carbonization treatment system | |
| CN102049171A (en) | Method for reclaiming and treating hydrocarbon-containing waste gas | |
| CN104556281B (en) | A kind of method removing the carbon dioxide contained in water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20171013 |