CN108277042A - A kind of hot tank feed process of intermediate products and its system - Google Patents
A kind of hot tank feed process of intermediate products and its system Download PDFInfo
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- CN108277042A CN108277042A CN201810363925.0A CN201810363925A CN108277042A CN 108277042 A CN108277042 A CN 108277042A CN 201810363925 A CN201810363925 A CN 201810363925A CN 108277042 A CN108277042 A CN 108277042A
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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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
-
- 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
-
- 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
- B01D53/75—Multi-step processes
-
- 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
-
- 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
-
- 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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
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- 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)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of hot tank feed process of intermediate products, including a hot tank charging/discharging process and a Volatile Gas removal process.The concrete scheme of this method is：By the intermediate products of atmospheric unit, catalytic unit and coking plant production without air-cooled or water cooling, Direct Classification enters the hot tank of diesel oil and the hot tank of wax oil carries out homogeneous, samming, measures and purify, hot tank nitrogen injection isolation oil is contacted with air, the moisture of vaporization and the oil gas of volatilization are recycled, removing moisture, light oil and lighter hydrocarbons gas, hot material enter downstream unit with 100 180 DEG C of temperature.High warm tank is arranged in the present invention between upstream and downstream device, the advantages of having cold tank charging and hot material direct-furnish charging concurrently can eliminate the influence of the fluctuation of upstream and downstream device and operation troubles to operation, can realize hot feed, also charging can be purified and be stablized, safe and stable and energy-efficient effect is reached.The present invention additionally provides the system for realizing this method simultaneously.
Description
Technical field
The invention belongs to petrochemical industry field of energy-saving technology, and in particular to a kind of hot tank feed process of intermediate products, this hair
It is bright to also relate to a kind of system for realizing this method.
Background technology
For petrochemical industry oil refining apparatus, energy consumption is directly related to the overall operation level of oil refining enterprise and economic effect
Benefit.Heat integration between device be by two sets of upstream and downstream or more covering devices as a whole, according to " temperature equity, step profit
With " principle carry out the matching of " high fever height use, the low use of low-heat ", reduce process exergy loss, save recirculated water and fuel gas,
20-40% generally is can save energy, therefore is effective energy saving way.
Hot feed is the tie of heat integration, refers to the material the relation between supply and demand between device, the product stream of upstream device without
Supercooling is not exclusively cooling, is directed directly to downstream unit as hot feed.Currently, feeding manner has cold tank charging and hot material
Direct-furnish feeds two kinds, respectively there is advantage and disadvantage.Cold tank charging refers to intermediate products（Diesel component or wax oil component）Through cooling discharging
To intermediate storage tank, diesel component is cooled to 70 DEG C hereinafter, wax oil component is cooled to 90 DEG C hereinafter, being sent again to downstream through intermediate storage tank
Device, this feeding manner can make to keep relatively independent by intermediate storage tank between upstream and downstream device, not interfere with each other, intermediate products
Water can be cut with standing sedimentation, this traditional design being thermally isolated by intermediate storage tank implementation between device has stronger operation
Flexibility, safety, stability and good reliability.The disadvantage is that linking upstream and downstream device intermediate products must first through cooling,
It heats up again, experience heat exchange twice and the loss of two-stage available energy cause plant energy consumption high, moreover, because intermediate products are containing unsaturation
Alkene, alkene is contacted with the air in intermediate storage tank gas-phase space can occur oxidation reaction generation colloid, increase purpose product
Loss and hydrogen consumption block the duct of hydrogenation catalyst, shorten catalyst service life；Another feeding manner is that hot material is straight
For charging, refers to that intermediate products discharge from upstream device heat, without air-cooled and cooling by water, is fed directly to downstream unit,
This feed mode can save the recirculated water of upstream device and the fuel of downstream unit, be conducive to it is energy saving, the disadvantage is that
Upstream and downstream device material directly mutually supplies, highly relevant between device, interfere with each other, to existing operation, control, safety guarantee etc.
Larger impact can be brought, there are security risk, moreover, because the operations such as upstream device water filling, steam injection, stripping, because of centre
Product is the aromatic hydrocarbons hydrophilic radical of oil-containing, unavoidably carries moisture, while also containing a small amount of light hydrocarbon component and light oil constituents,
Downstream unit is necessarily caused to be difficult to precisely adjustment and edge operation.
《Energy research and management》1st phase 53-55 in 2010 once disclosed entitled " heat integration of oil refining apparatus and a heat
The article of feed ", article elaborate heat integration principle, describe and promote the material mutually application of confession and implementation heat integration, text
Hot tank feed process is not referred in chapter.
《Petroleum refining and chemical industry》The 8th phase 56-61 of volume 41 in 2010 once disclosed entitled " hot feed promotion plus a hydrogen
Device gos deep into energy saving optimizing " article, article elaborates to push hydrogenation plant fully optimized by opportunity of hot feed, but not carry
And hot tank feed process.
Chinese patent CN103363295 A disclose " a kind of hot method of feeding of process product diesel oil ", which is upper
Heat feed distribution station is established between downstream unit, and the discharging of same type logistics heat is concentrated to the hot method of feeding of distribution station, collection
The middle assisting workflows for considering process accident, relatively conventional hot material direct-furnish method improve to some extent, but it to be that flow lacks that there are problems
Hot flexibility, the operation fluctuation of upstream device and equipment fault direct interference downstream unit, it is difficult to realize fine operation adjustment,
In the case where upstream device operates fluctuation and accident condition, must be stored after cooling into cold tank.
Chinese patent CN204455008 U disclose " a kind of hot feeding device of diesel oil ", which discloses
On the basis of traditional hot material direct-furnish method, increases a heat and go out stockline and upstream device liquid level is jointly controlled, which does not have yet
Refer to hot tank feed process.
In conclusion in existing fed technology, cold tank charging and hot material direct-furnish feed two ways and deposit, and exist not
Foot place.
Invention content
An object of the present invention is to provide a kind of hot tank feed process of intermediate products, and this method has cold tank feed process concurrently
The advantages of with hot material direct-furnish feed process, overcomes the deficiency of the two, and operation is flexible greatly, low energy consumption, security and stability is good.
The above-mentioned purpose of the present invention is achieved by the following technical solution：More particularly to a kind of hot tank of intermediate products into
Material method, which is characterized in that this method includes a hot tank charging/discharging process and a Volatile Gas removal process, wherein
The hot tank charging/discharging process includes the following steps：
（1）The intermediate products come from upstream device, cool down without air-cooled or cooling by water, with higher temperature（100~180
℃）Into static mixer, temperature and uniform properties into hot tank are made by mixing；
（2）Intermediate products settle and stand purification, diesel component storage temperature 100~155 in hot tank high-temperature storage, into row buffering
DEG C, 100~180 DEG C of wax oil component storage temperature, hot tank mean residence time 3~6 days；
The solid impurity carried from upstream device is settled down to hot tank tank bottom, is cleared up in shut-down (breakdown) mainteance, entrained moisture,
Low-boiling light oil and sl. sol. lighter hydrocarbons gas（Refer mainly to liquefied gas and device in Gas）, during hot material quiescence in high temperature vaporization or
It releases, into the gas-phase space on hot tank top, realizes hot material dehydration, de- light oil and de- lighter hydrocarbons gas；
（3）Intermediate products after overheat tank homogeneous samming and dehydration degassing, extract out from hot pot bottom and are pressurized by feed pump, sent
Enter downstream unit processing.
Heretofore described upstream device refers to atmospheric unit, catalytic unit and coking plant, and the downstream unit refers to
Hydro-refining unit, hydro-upgrading unit or hydrocracking unit.
Heretofore described intermediate products refer to diesel component or wax oil component, and diesel component includes atmospheric unit production
Ordinary pressure diesel, catalytic unit production catalytic diesel oil and coking plant production coker gas oil, boiling range ranging from 180~365
℃；Wax oil component includes the normal pressure wax oil of atmospheric unit production, the catalysis heavy-cycle oil of catalytic unit production and coking plant life
The wax tailings of production, ranging from 350~500 DEG C of boiling range, intermediate products divide tank thermmal storage according to diesel component and wax oil component.
The Volatile Gas removal process includes the following steps：
（1）Nitrogen is passed through by pressure control in hot tank top, full of gas-phase space inside hot tank, maintains gaseous pressure in hot tank
In 300Pa（Table）Left and right, being in direct contact for oil product and air is isolated；
（2）The moisture of vaporization and the oil gas of volatilization come out from hot tank top, by single breathing valve, anti-Hong type spark arrester, are drawn by frequency conversion
Wind turbine boosting, which is sent to water cooler, to be cooled down, and frequency converting induced draft fan is carried out automatically controlling by the pressure of oil-gas pipeline, when inlet pressure height
In 300Pa（Table）When, frequency converting induced draft fan starts, when inlet pressure is less than -300 Pa（Table）When, frequency converting induced draft fan is out of service；
The level pressure value of single breathing valve is 1100Pa（Table）, when hot tank deck pressure is higher than 1200Pa（Table）When, single breathing valve is opened, when hot tank deck pressure
Power is less than 1000Pa（Table）When, single breathing valve is closed；
（3）Oil gas is cooled to 20~40 DEG C by water cooler, and water, oil and qi leel are carried out from condensing out into three phase separation tank
Sewage acidic water stripping device be intermittently pumped to by sewage be pocessed, light oil is intermittently sent by light oil pump to tank field light oil
Tank, lighter hydrocarbons gas is into desulfurizing tower；
（4）Lighter hydrocarbons gas is into desulfurizing tower bottom of tower, with the concentration 5~15% for coming from tower top（Mass concentration）Sodium hydroxide sig water
Counter current contacting removes the sulphur impurity in lighter hydrocarbons gas, and the lighter hydrocarbons gas after desulfurization is emitted into gas holder by low pressure gas pipe network, then passes through
Gas holder is recycled；Sig water is recycled by lye pump, waits for that concentration of lye is reduced to 5%（Mass concentration）When following,
Note alkali is made by lye pump pressure-increasing unit to acidic water stripping device.
It is a further object to provide a kind of hot tank feed system of intermediate products, which can realize oil product high temperature
Safe storage, the influence by the fluctuation of hot tank snubber upstream and downstream device and operation troubles to operation, can realize hot feed,
Also charging can be purified and stablize, and safe and reliable.
This purpose of the present invention is realized by the following technical solutions：A kind of intermediate products hot tank charging system
System comprising hot tank charging/discharging unit, Volatile Gas recovery unit, nitrogen envelope voltage-controlled valve and double exhale valve, which is characterized in that the hot tank
Disengaging material unit, Volatile Gas recovery unit, nitrogen envelope voltage-controlled valve and it is double exhale valve group close installation, intermediate products from upstream device come with compared with
High-temperature（100~180 DEG C）High-temperature storage is carried out into the hot tank charging/discharging unit, buffered standing purifies laggard downstream dress
It sets, the water of vaporization and the oil gas of volatilization carry out condensation water removal, caustic wash desulfuration into the Volatile Gas recovery unit, recycling light oil and light
The hydrocarbon gas, nitrogen inject contact of the hot tank charging/discharging cell isolation air with oil gas by nitrogen envelope voltage-controlled valve, and described pair is exhaled
Valve is security implementation, avoid hot tank build the pressure or take out it is flat.
Hot tank charging/discharging unit of the present invention include pass sequentially through pipeline connection first via intermediate products control valve,
Second road intermediate products control valve, third road intermediate products control valve, static mixer, hot tank, feed pump, inlet control valve,
Charge filter and downstream unit, the first via intermediate products control valve, the second road intermediate products control valve and third road
Intermediate products control valve is in parallel；The hot tank top be provided with nitrogen envelope import, it is double exhale valve be open and single breathing valve opening, the hot tank
Side be provided with hot tank feed inlet, hot tank discharge port and hot tank sewage draining exit, the hot tank feed inlet is in the epimere of hot tank, the warm
Tank discharge port is opened in the tank bottom of hot tank at about 0.5m, the hot tank sewage draining exit hot tank tank bottom, the hot tank feed inlet with
Hot tank discharge port is mutually 180 degree along the radial direction of hot tank, with the hot tank sewage draining exit at 90 degree；The described nitrogen envelope import with it is described
Nitrogen seal voltage-controlled valve outlet, the single breathing valve is connected to the hot tank Volatile Gas recovery unit, and described pair is exhaled valve
Arrival end exhales valve open communication, outlet end and atmosphere with the double of hot tank top.
Further, the hot 5000~30000m of tank volume3, using vault construction, design normal pressure is 3000 Pa
（Table）, -500 Pa of negative pressure（Table）.
Further, it is described it is double to exhale valve be emergency discharge safety devices, it is double that exhale valve level pressure value be 1765Pa（Table）, when hot tank
Pressure on top surface is higher than 1940Pa（Table）When, it is double that valve is exhaled to open exhaust outward, when hot tank deck pressure is less than 1605Pa（Table）When, it is double to exhale valve
It closes, when hot tank deck pressure is less than -294Pa（Table）When, it is double to exhale valve to open to supplement air into hot tank, prevent hot tank from building the pressure or taking out
It is flat.
Further, the tank deck heat preservation of the hot tank uses micro-nano thermal insulation board（3mm）+ vacuum forming ceramic beaverboard
（60mm）Insulating layer, outer layer coated with hard polyurethane water barrier+metal color steel protection, tank skin heat preservation are micro-nano heat-insulated using serving as a contrast
Plate（3mm）+ vacuum forming ceramic beaverboard（180mm）+ metal color steel is protected, to ensure that insulating layer hull-skin temperature is less than 50
DEG C, reduce heat loss.
Further, the hot tank is sealed using nitrogen, is carried out automatically controlling with hot tank deck pressure, isolation air and oil product in tank
It is in direct contact, avoids unsaturated hydrocarbons contained in the oxygen and intermediate products in air that oxidation life occurs during high-temperature storage
Collagen or other oxygen carriers cause hydrogen consumption increase, the blocking of catalyst duct and equipment scaling, influence downstream unit
The service life of the cycle of operation and catalyst.
Volatile Gas recovery unit of the present invention is at the purification of the light oil and lighter hydrocarbons gas that recycle the moisture, volatilization that vaporize
Manage device comprising the single breathing valve opening that is sequentially communicated by pipeline, single breathing valve, anti-detonation type spark arrester, frequency converting induced draft fan, water
Cooler, three phase separation tank, desulfurizing tower and lighter hydrocarbons gas takeoff line composition, the three phase separation tank bottom dehydration packet outlet are pumped into sewage
Mouthful be connected, sewage is intermittently delivered to acidic water stripping device by the sewage pump, the three phase separation pot bottom outlet with
Light oil pump intake is connected, and light oil is intermittently delivered to light oil tank field, the three phase separation tank top by light oil pump supercharging
Outlet is connected with desulfurizing tower bottom air inlet, and solidifying lighter hydrocarbons gas does not enter from desulfurization tower bottom；The desulfurizing tower top exit
It is connected to lighter hydrocarbons gas takeoff line, the desulfurizing tower outlet at bottom is connected to lye pump arrival end, and the lye pump discharge bifurcates
Pipeline, the first branch pipe(tube) are connected to lye import at the top of desulfurizing tower, and the second branch pipe(tube) connects sewage stripping and notes alkali tank.
Further, the desulfurizing tower is packed tower, concentration 5~15%（Mass concentration）Sodium hydroxide lye by lye pump
Supercharging, by lye circular route at the top of desulfurizing tower with from desulfurization tower bottom into lighter hydrocarbons gas in desulfurizing tower counter current contacting, take off
Sulphide removal, the lighter hydrocarbons gas after desulfurization are ejected from desulfurizing tower, enter low pressure gas pipe network, lye cycle by lighter hydrocarbons gas takeoff line
It uses, is less than 5% in concentration of lye（Mass concentration）When, acidic water stripping device is intermittently delivered to by lye pump supercharging and is used as
Note alkali.
The present invention is to have cold tank charging and hot material concurrently into row buffering sedimentation, standing purification and homogeneous samming by hot tank
The advantages of direct-furnish is fed.Compared with prior art, the present invention has following remarkable result：
（1）Ensure that downstream unit feed properties are stablized.It, can balanced raw material since hot tank volume is big compared with hot material direct-furnish is fed
The fluctuation of property, composition, temperature and flow ensures that downstream unit feed rate, temperature and property are stablized, and is that downstream unit is fine
Adjustment and edge operation provide strong guarantee.
（2）Purify downstream unit charging.Compared with hot material direct-furnish is fed, the present invention is stored up by hot material in hot tank high temperature
It deposits, impurity, light oil and the lighter hydrocarbons gas entrained by upstream device is removed and recycled, downstream unit charging is purified, from
And eliminate influence of the upstream raw material impurity to the produce load of downstream unit, catalyst, hydrogen consumption and long-term operation.
（3）It is energy-saving.Compared with cold tank is fed, by heat integration between hot tank progress device, deactivated upstream device water cooling,
It is air-cooled, recirculated water is saved, fuel gas is reduced, 20% or more energy consumption can be saved；Connecing for exhausted oil product and air is insulated by hot tank nitrogen
It touches, inhibits the generation of colloid, and then reduce hydrogen consumption, being recycled by Volatile Gas reduces oil product loss.
（4）Stability, safety and reliability are good.Compared with hot material direct-furnish is fed, upstream and downstream device is realized by hot tank
Hot flexible connection, the independence operated between device maximize the retention, by the powerful surge volume of hot tank, can delay
Any operation fluctuation and the operation troubles of upstream and downstream device are received in suction, resist accident and operation fluctuation ability is strong.
A kind of hot tank feed process of intermediate products of the present invention and device can be used for diesel oil, wax oil, residual oil heat into
Material process or combinations thereof process, therefore the invention is practical, has great application prospect.
Description of the drawings
Fig. 1 is the process flow diagram of the present invention；
Fig. 2 is the structural schematic diagram of hot tank in Fig. 1；
Symbol description：1. first via intermediate products control valve；2. the second road intermediate products control valve；3. the intermediate products control of third road
Valve processed；4. static mixer；5. hot tank；6. feed pump；7. inlet control valve；8. charge filter；9. downstream unit；10. nitrogen
Seal voltage-controlled valve；11. pair exhaling valve；12. single breathing valve；13. anti-detonation type spark arrester；14. frequency converting induced draft fan；15. water cooler；16. three
Phase separation pot；17. sewage pump；18. sewage output line；19. light oil pumps；20. light oil export pipeline；21. desulfurizing tower；22. lye
Pump；23. alkaline residue output line；24. lye pipeloop；25. lighter hydrocarbons gas takeoff line；51. hot tank feed inlet；52. nitrogen seals import；
53. pair valve is exhaled to be open；54. single breathing valve is open；55. hot tank discharge port；56. hot tank sewage draining exit.
Specific implementation mode
As shown in Figure 1 and Figure 2, the hot tank feed system of a kind of intermediate products comprising hot tank charging/discharging unit, Volatile Gas are returned
It receives unit, nitrogen envelope voltage-controlled valve 10 and double exhales valve 11, which is characterized in that the hot tank charging/discharging unit, Volatile Gas recovery unit, nitrogen
Envelope voltage-controlled valve 10 exhales the combination installation of valve 11, intermediate products to come from upstream device with higher temperature with double（100~180 DEG C）Into described
Hot tank charging/discharging unit carry out high-temperature storage, the laggard downstream unit of buffered standings purification, the water of vaporization and the oil gas of volatilization into
The Volatile Gas recovery unit carries out condensation water removal, caustic wash desulfuration, recycles light oil and lighter hydrocarbons gas, and nitrogen seals voltage-controlled valve by the nitrogen
Contact of the 10 injection hot tank charging/discharging cell isolation air with oil gas, it is security implementation that described pair, which is exhaled valve 11, avoids hot tank 5
It builds the pressure or takes out and is flat.
Hot tank charging/discharging unit of the present invention includes the first via intermediate products control valve for passing sequentially through pipeline connection
1, the second road intermediate products control valve 2, third road intermediate products control valve 3, static mixer 4, hot tank 5, feed pump 6, charging
Control valve 7, charge filter 8 and downstream unit 9, the first via intermediate products control valve 1, the second road intermediate products control
Valve 2 and third road intermediate products control valve 3 are in parallel；5 top of the hot tank is provided with the import 52 of nitrogen envelope, double valve openings 53 and single of exhaling
Valve opening 54 is exhaled, the side of the hot tank 5 is provided with hot tank feed inlet 51, hot tank discharge port 55 and hot tank sewage draining exit 56, the heat
In the epimere of hot tank 5, the hot tank discharge port 55 is opened in the tank bottom of hot tank 5 at about 0.5m tank feed inlet 51, the hot tank row
For dirty mouth 56 in the tank bottom of hot tank 5, the hot tank feed inlet 51 and hot tank discharge port 55 be mutually 180 degree along the radial direction of hot tank 5, with
The hot tank sewage draining exit 56 is at 90 degree；The nitrogen envelope import 52 seals 10 outlet of voltage-controlled valve, the list with the nitrogen
Valve 12 is exhaled to be connected to the Volatile Gas recovery unit, described pair is exhaled the arrival end of valve 11 to exhale valve to be open with the double of 5 top of hot tank
53 connections, outlet end and atmosphere.
Further, the 5 5000~30000m of volume of hot tank3, using vault construction, design normal pressure is 3000 Pa
（Table）, -500 Pa of negative pressure（Table）.
Further, it is described it is double to exhale valve 11 be emergency discharge safety devices, it is double that exhale 11 level pressure value of valve be 1765Pa（Table）, when
5 pressure on top surface of hot tank is higher than 1940Pa（Table）When, it is double that valve 11 is exhaled to open outside exhaust, when 5 pressure on top surface of hot tank is less than 1605Pa（Table）
When, it is double that valve 11 is exhaled to close, when 5 pressure on top surface of hot tank is less than -294Pa（Table）When, it is double to exhale valve 11 to open to supplement air into hot tank 5,
Prevent hot tank 5 build the pressure or take out it is flat.
Further, the tank deck heat preservation of the hot tank 5 uses micro-nano thermal insulation board（3mm）+ vacuum forming ceramic beaverboard
（60mm）Insulating layer, outer layer coated with hard polyurethane water barrier+metal color steel protection, tank skin heat preservation are micro-nano heat-insulated using serving as a contrast
Plate（3mm）+ vacuum forming ceramic beaverboard（180mm）+ metal color steel is protected, to ensure that insulating layer hull-skin temperature is less than 50
DEG C, reduce heat loss.
Further, the hot tank 5 is sealed using nitrogen, is carried out automatically controlling with 5 pressure on top surface of hot tank, isolation air and oil in tank
Product are in direct contact, and unsaturated hydrocarbons contained in oxygen and intermediate products in air is avoided to be aoxidized during high-temperature storage
Colloid or other oxygen carriers are generated, hydrogen consumption increase, the blocking of catalyst duct and equipment scaling is caused, influences downstream unit
The cycle of operation and catalyst service life.
Further, 5 tank deck of hot tank is sealed using nitrogen, and pressure signal takes 5 tank deck pressure of hot tank to carry out automatically controlling, every
Exhausted air is in direct contact with oil product in tank, avoids unsaturated hydrocarbons contained in the oxygen and intermediate products in air in high-temperature storage
Oxidation occurs in the process and generates colloid or other oxygen carriers, causes hydrogen consumption to increase, catalyst duct blocks and equipment knot
Dirt influences the cycle of operation of downstream unit, the service life of refining losses and catalyst.
Volatile Gas recovery unit of the present invention is the light oil and lighter hydrocarbons for recycling the moisture, volatilization that are vaporized from hot tank 5
The purifying processing device of gas comprising individual calling valve outlet 54, single breathing valve 12, the anti-detonation type spark arrester being sequentially communicated by pipeline
13, frequency converting induced draft fan 14, water cooler 15, three phase separation tank 16, desulfurizing tower 21 and lighter hydrocarbons gas takeoff line 25 form, the three-phase separate
Packet outlet is dehydrated from 16 bottom of tank with 17 entrance of sewage pump to be connected, sewage intermittently passes through sewage output line by the sewage pump 17
18 are delivered to acidic water stripping device；16 outlet at bottom of three phase separation tank pumps 19 entrances with light oil and is connected, and light oil is by institute
It states 19 supercharging of light oil pump and light oil tank field is intermittently delivered to by light oil export pipeline 20；16 top exit of three phase separation tank
It is connected with 21 bottom air inlet of desulfurizing tower, solidifying lighter hydrocarbons gas does not enter from 21 bottom of desulfurizing tower；21 top of the desulfurizing tower goes out
Mouth is connected to by lighter hydrocarbons gas takeoff line 25 with low pressure gas pipe network, and 21 outlet at bottom of the desulfurizing tower connects with 22 arrival end of lye pump
Logical, the outlet of the lye pump 22 divides two-way, first via pipeline to be lye pipeloop 24, connects with 21 top lye import of desulfurizing tower
Logical, the second road pipeline is alkaline residue output line 23, is connected to sewage stripping note alkali tank.
Further, the desulfurizing tower 21 is packed tower, concentration 5-15%（Mass concentration）Sodium hydroxide lye by lye pump
22 superchargings are delivered to the top of desulfurizing tower 21 by lye circular route 24, with from 21 bottom of desulfurizing tower into lighter hydrocarbons gas in desulfurizing tower
Counter current contacting in 21 removes sulfide, and the lighter hydrocarbons gas after desulfurization enters low pressure gas pipe network by lighter hydrocarbons gas takeoff line 25, from tower
The lye of bottom extraction recycles, and is less than 5% in concentration of lye（Mass concentration）When, it is pressurized by lye pump 22, is exported by alkaline residue
Line 23 is intermittently delivered to acidic water stripping device and is used as note alkali.
The method for carrying out the hot tank charging of intermediate products using above system, this method can be divided into hot tank charging/discharging process and wave
It gets angry removal process, wherein
The hot tank charging/discharging process includes the following steps：
（1）The intermediate products come from upstream device, cool down without air-cooled or cooling by water, with higher temperature（100~180
℃）Into static mixer, temperature and uniform properties into hot tank are made by mixing；
（2）Intermediate products settle and stand purification, diesel component storage temperature 100~155 in hot tank high-temperature storage, into row buffering
DEG C, 100~180 DEG C of wax oil component storage temperature, hot tank mean residence time 3~6 days；
The solid impurity carried from upstream device is settled down to hot tank tank bottom, is cleared up in shut-down (breakdown) mainteance, entrained moisture content,
Low-boiling light oil and sl. sol. lighter hydrocarbons gas（Refer mainly to liquefied gas and device in Gas）During hot tank quiescence in high temperature, vaporization or
It releases, into the gas-phase space on hot tank top, realizes dehydration, de- light oil and de- lighter hydrocarbons gas；
（3）Intermediate products after overheat tank homogeneous samming and dehydration degassing, extract out from hot pot bottom and are pressurized by feed pump, sent
Enter downstream unit processing.
Heretofore described upstream device refers to atmospheric unit, catalytic unit and coking plant, and the downstream unit refers to
Hydro-refining unit, hydro-upgrading unit or hydrocracking unit.
Heretofore described intermediate products refer to diesel component or wax oil component, and diesel component includes atmospheric unit production
Ordinary pressure diesel, catalytic unit production catalytic diesel oil, coking plant production coker gas oil, boiling range ranging from 180~365
℃；Wax oil component includes the normal pressure wax oil of atmospheric unit production, the catalysis heavy-cycle oil of catalytic unit production, coking plant production
Wax tailings, ranging from 350~500 DEG C of boiling range, intermediate products divide tank thermmal storage according to diesel component and wax oil component.
The Volatile Gas removal process includes the following steps：
（1）Nitrogen is passed through by pressure control in hot tank top, full of gas-phase space inside hot tank, maintains gaseous pressure in hot tank
In 300Pa（Table）Left and right, being in direct contact for oil product and air is isolated；
（2）The moisture of vaporization and the oil gas of volatilization come out from hot tank top, by single breathing valve, anti-detonation type spark arrester, by frequency conversion
Air-introduced machine boosting, which is sent to water cooler, to be cooled down, and frequency converting induced draft fan is carried out automatically controlling by the pressure of oil-gas pipeline, works as inlet pressure
Higher than 300Pa（Table）When, frequency converting induced draft fan starts, when inlet pressure is less than -300 Pa（Table）When, frequency converting induced draft fan stops fortune
Row；The level pressure value of single breathing valve is 1100Pa（Table）, it is higher than 1200Pa in hot tank deck pressure（Table）When, single breathing valve is opened, when hot tank
Pressure on top surface is less than 1000Pa（Table）When, single breathing valve is closed；
（3）Oil gas cools down 20~40 DEG C by water cooler, and water, oil and qi leel are carried out from condensing out into three phase separation tank
Sewage is intermittently pumped to sewage stripping by sewage and is pocessed, and light oil is intermittently sent to tank field light oil tank, gently by light oil pump
The hydrocarbon gas is into desulfurizing tower；
（4）Lighter hydrocarbons gas is into desulfurizing tower bottom of tower, with the concentration 5~15% for coming from tower top（Mass concentration）Sodium hydroxide sig water
Counter current contacting removes the sulphur impurity in lighter hydrocarbons gas, and the lighter hydrocarbons gas after desulfurization is emitted into gas holder by low pressure gas pipe network, then passes through
Gas holder is recycled.Sig water is recycled by lye pump, waits for that concentration of lye is reduced to 5%（Mass concentration）When following,
Note alkali is made by lye pump pressure-increasing unit to acidic water stripping device.
Embodiment 2
Unlike embodiment 1, upstream device intermediate products in the present embodiment be atmospheric and vacuum distillation unit production decompressed wax oil,
The catalysis heavy-cycle oil of catalytic unit production, the wax tailings of coking plant production, ranging from 350-500 DEG C of boiling range.Downstream fills
It is set to wax oil hydrogenation modifying apparatus, operating pressure 13.8MPa（Table）, removing sulphur, nitrogen impurity, and to polycyclic in wax oil component
Aromatic hydrocarbons carries out depth saturation, mononuclear aromatics is generated, as good fcc raw material.
The method for carrying out the hot tank charging of wax oil component using the device of the present embodiment, this method can be divided into hot tank charging/discharging mistake
Journey and Volatile Gas removal process, wherein
The hot tank charging/discharging process includes the following steps：
（1）The intermediate products come from upstream device, cool down without air-cooled or cooling by water, enter static mix for 170 DEG C with temperature
Clutch makes temperature and uniform properties into hot tank by mixing；
（2）Intermediate products settle and stand purification, 170 DEG C of wax oil component storage temperature, heat in hot tank high-temperature storage, into row buffering
Tank mean residence time 3 days；
The solid impurity carried from upstream device is settled down to hot tank tank bottom, is cleared up in shut-down (breakdown) mainteance, entrained moisture,
Low-boiling light oil and sl. sol. lighter hydrocarbons gas are vaporized or are released during hot material quiescence in high temperature, into hot tank top
Gas-phase space, realize dehydration, de- light oil and de- lighter hydrocarbons gas；
（3）Intermediate products after overheat tank homogeneous samming and dehydration degassing, extract out from hot pot bottom and are pressurized by feed pump, sent
Enter downstream wax oil hydrogenation modifying apparatus processing.
The Volatile Gas removal process includes the following steps：
（1）Nitrogen is passed through by pressure control in hot tank top, full of gas-phase space inside hot tank, maintains gaseous pressure in hot tank
In 300Pa（Table）Left and right, being in direct contact for oil product and air is isolated；
（2）The moisture of vaporization and the oil gas of volatilization come out from hot tank top, by single breathing valve, anti-detonation type spark arrester, by frequency conversion
Air-introduced machine boosting, which is sent to water cooler, to be cooled down, and frequency converting induced draft fan is carried out automatically controlling by the pressure of oil-gas pipeline, works as inlet pressure
Higher than 300Pa（Table）When, frequency converting induced draft fan starts, when inlet pressure is less than -300 Pa（Table）When, frequency converting induced draft fan stops fortune
Row；The level pressure value of single breathing valve is 1100Pa（Table）, when hot tank deck pressure is higher than 1200Pa（Table）When, single breathing valve is opened, when hot tank
Pressure on top surface is less than 1000Pa（Table）When, single breathing valve is closed；
（3）Oil gas cools down 40 DEG C by water cooler, and water, oil and qi leel are carried out from the sewage condensed out into three phase separation tank
It is intermittently pumped to sewage stripping by sewage to be pocessed, light oil is intermittently sent by light oil pump to tank field light oil tank, lighter hydrocarbons gas
Into desulfurizing tower；
（4）Lighter hydrocarbons gas is into desulfurizing tower bottom of tower, with the concentration 15% for coming from tower top（Mass concentration）Sodium hydroxide sig water adverse current
Contact removes the sulphur impurity in lighter hydrocarbons gas, and the lighter hydrocarbons gas after desulfurization is emitted into gas holder by low pressure gas pipe network, then passes through gas holder
It is recycled；Sig water is recycled by lye pump, waits for that concentration of lye is reduced to 5%（Mass concentration）When following, by alkali
Liquid pump pressure-increasing unit to acidic water stripping device makees note alkali.
Embodiment 3
Unlike embodiment 2, the upstream device in the present embodiment is atmospheric unit, catalytic unit and coking plant, difference
Ordinary pressure diesel, catalytic diesel oil and coker gas oil, ranging from 180-365 DEG C of boiling range are produced, downstream unit fills for diesel oil hydrofining
It sets, hydrogenation pressure 10.0MPa（Table）, removing sulphur, nitrogen impurity and aromatic hydrocarbons depth saturation, producing country's V derv fuels.
The method for carrying out the hot tank charging of diesel component using the device of the present embodiment, this method can be divided into hot tank charging/discharging mistake
Journey and Volatile Gas removal process, wherein
The hot tank charging/discharging process includes the following steps：
（1）The intermediate products diesel component come from upstream device, cools down without air-cooled or cooling by water, with 155 DEG C of temperature into
Enter static mixer, temperature and uniform properties into hot tank are made by mixing；
（2）Intermediate products settle and stand purification, 155 DEG C of diesel component storage temperature, heat in hot tank high-temperature storage, into row buffering
Tank mean residence time 6 days；
The solid impurity carried from upstream device is settled down to hot tank tank bottom, is cleared up in shut-down (breakdown) mainteance, entrained moisture,
Low-boiling light oil and sl. sol. lighter hydrocarbons gas are vaporized or are released during hot material quiescence in high temperature, into hot tank top
Gas-phase space, realize dehydration, de- light oil and de- lighter hydrocarbons gas；
（3）Intermediate products after overheat tank homogeneous samming and dehydration degassing, extract out from hot pot bottom and are pressurized by feed pump, sent
Enter downstream unit processing.
The Volatile Gas removal process includes the following steps：
（1）Nitrogen is passed through by pressure control in hot tank top, full of gas-phase space inside hot tank, maintains gaseous pressure in hot tank
In 300Pa（Table）Left and right, being in direct contact for oil product and air is isolated；
（2）The moisture of vaporization and the oil gas of volatilization come out from hot tank top, by single breathing valve, anti-detonation type spark arrester, by frequency conversion
Air-introduced machine boosting, which is sent to water cooler, to be cooled down, and frequency converting induced draft fan is carried out automatically controlling by the pressure of oil-gas pipeline, works as inlet pressure
Higher than 300Pa（Table）When, frequency converting induced draft fan starts, when pressure is less than -300 Pa（Table）When, frequency converting induced draft fan is out of service；It is single
It is 1100Pa to exhale the level pressure value of valve（Table）, when hot tank deck pressure is higher than 1200Pa（Table）When, single breathing valve is opened, when hot tank deck pressure
Less than 1000Pa（Table）When, single breathing valve is closed；
（3）Oil gas cools down 35 DEG C by water cooler, and water, oil and qi leel are carried out from the sewage condensed out into three phase separation tank
It is intermittently pumped to acidic water stripping device by sewage to be pocessed, light oil is intermittently sent to tank field light oil tank, gently by light oil pump
The hydrocarbon gas is into desulfurizing tower；
（4）Lighter hydrocarbons gas is into desulfurizing tower bottom of tower, with the concentration 10% for coming from tower top（Mass concentration）Sodium hydroxide sig water adverse current
Contact removes the sulphur impurity in lighter hydrocarbons gas, and the lighter hydrocarbons gas after desulfurization is emitted into gas holder by low pressure gas pipe network, then passes through gas holder
It is recycled, sig water is recycled by lye pump, waits for that concentration of lye is reduced to 5%（Mass concentration）When following, by alkali
Liquid pump pressure-increasing unit to acidic water stripping device makees note alkali.
All documents that the present invention refers to are incorporated herein by reference, and are individually drawn just as each document
It is used as with reference to such.In addition, it should also be understood that, after reading the above teachings of the present invention, those skilled in the art can be with
The present invention is made various changes or modifications, such equivalent forms equally fall within model defined by the application the appended claims
It encloses.
Claims (10)
1. a kind of hot tank feed process of intermediate products, which is characterized in that this method includes a hot tank charging/discharging process and one
Volatile Gas removal process, wherein
The hot tank charging/discharging process includes the following steps：
（1）The intermediate products come from upstream device, cool down without air-cooled or cooling by water, with higher temperature（100~180
℃）Into static mixer, temperature and uniform properties into hot tank are made by mixing；
（2）Intermediate products settle and stand purification, diesel component storage temperature 100~155 in hot tank high-temperature storage, into row buffering
DEG C, 100~180 DEG C of wax oil component storage temperature, hot tank mean residence time 3~6 days；
The solid impurity carried from upstream device is settled down to hot tank tank bottom, is cleared up in shut-down (breakdown) mainteance, entrained moisture,
Low-boiling light oil and sl. sol. lighter hydrocarbons gas（Refer mainly to liquefied gas and device in Gas）, during hot material quiescence in high temperature vaporization or
It releases, into the gas-phase space on hot tank top, realizes hot material dehydration, de- light oil and de- lighter hydrocarbons gas；
（3）Intermediate products after overheat tank homogeneous samming and dehydration degassing, extract out from hot pot bottom and are pressurized by feed pump, sent
Enter downstream unit processing；
The Volatile Gas removal process includes the following steps：
（1）Nitrogen is passed through by pressure control in hot tank top, full of gas-phase space inside hot tank, maintains gaseous pressure in hot tank
In 300Pa（Table）Left and right, being in direct contact for oil product and air is isolated；
（2）The moisture of vaporization and the oil gas of volatilization come out from hot tank top, by single breathing valve, anti-Hong type spark arrester, are drawn by frequency conversion
Wind turbine boosting, which is sent to water cooler, to be cooled down, and frequency converting induced draft fan is carried out automatically controlling by the pressure of oil-gas pipeline, when inlet pressure height
In 300Pa（Table）When, frequency converting induced draft fan starts, when inlet pressure is less than -300 Pa（Table）When, frequency converting induced draft fan is out of service；
The level pressure value of single breathing valve is 1100Pa（Table）, when hot tank deck pressure is higher than 1200Pa（Table）When, single breathing valve is opened, when hot tank deck pressure
Power is less than 1000Pa（Table）When, single breathing valve is closed；
（3）Oil gas is cooled to 20~40 DEG C by water cooler, and water, oil and qi leel are carried out from condensing out into three phase separation tank
Sewage acidic water stripping device be intermittently pumped to by sewage be pocessed, light oil is intermittently sent by light oil pump to tank field light oil
Tank, lighter hydrocarbons gas is into desulfurizing tower；
（4）Lighter hydrocarbons gas is into desulfurizing tower bottom of tower, with the concentration 5~15% for coming from tower top（Mass concentration）Sodium hydroxide sig water
Counter current contacting removes the sulphur impurity in lighter hydrocarbons gas, and the lighter hydrocarbons gas after desulfurization is emitted into gas holder by low pressure gas pipe network, then passes through
Gas holder is recycled；Sig water is recycled by lye pump, waits for that concentration of lye is reduced to 5%（Mass concentration）When following,
Note alkali is made by lye pump pressure-increasing unit to acidic water stripping device.
2. the hot tank feed process of a kind of intermediate products according to claim 1, which is characterized in that the intermediate products are
Refer to diesel component or wax oil component, diesel component include the ordinary pressure diesel of atmospheric unit production, catalytic unit production catalysis bavin
The coker gas oil that oil, coking plant produce, ranging from 180~365 DEG C of boiling range；Wax oil component includes the normal pressure of atmospheric unit production
The wax tailings of catalysis heavy-cycle oil, coking plant production that wax oil, catalytic unit produce, ranging from 350~500 DEG C of boiling range,
Intermediate products divide tank thermmal storage according to diesel component and wax oil component.
3. a kind of system for realizing a kind of hot tank feed process of intermediate products described in claim 1 comprising hot tank charging/discharging
Unit, Volatile Gas recovery unit, nitrogen envelope voltage-controlled valve and double exhale valve, which is characterized in that the hot tank charging/discharging unit, Volatile Gas are returned
Receive unit, nitrogen envelope voltage-controlled valve and it is double exhale valve group to close installation, intermediate products come from upstream device with higher temperature（100~180 DEG C）
High-temperature storage is carried out into the hot tank charging/discharging unit, buffered standing purifies laggard downstream unit, water and the volatilization of vaporization
Oil gas carries out condensation water removal, caustic wash desulfuration into the Volatile Gas recovery unit, recycles light oil and lighter hydrocarbons gas, nitrogen are sealed by the nitrogen
Voltage-controlled valve injects contact of the hot tank charging/discharging cell isolation air with oil gas, and it is security implementation that described pair, which is exhaled valve, avoids heat
Tank builds the pressure or takes out flat.
4. the hot tank feed system of a kind of intermediate products according to claim 3, which is characterized in that the hot tank charging/discharging
Unit includes in the first via intermediate products control valve, the second road intermediate products control valve, third road for pass sequentially through pipeline connection
Between control of product valve, static mixer, hot tank, feed pump, inlet control valve, charge filter and downstream unit, described
Intermediate products control valve, the second road intermediate products control valve and third road intermediate products control valve are in parallel all the way；The hot tank
Top is provided with the import of nitrogen envelope, double exhales that valve is open and single breathing valve opening, the side of the hot tank are provided with hot tank feed inlet, the discharging of hot tank
Mouthful and hot tank sewage draining exit, in the epimere of hot tank, the hot tank discharge port is opened in the tank bottom of hot tank about the hot tank feed inlet
At 0.5m, in the tank bottom of hot tank, the hot tank feed inlet is mutually with hot tank discharge port along the radial direction of hot tank the hot tank sewage draining exit
180 degree, with the hot tank sewage draining exit at 90 degree；The nitrogen envelope import seals voltage-controlled valve outlet with the nitrogen, described
Single breathing valve be connected to the Volatile Gas recovery unit, it is described double the arrival ends of valve to be exhaled to exhale valve opening to connect with the double of hot tank top
It is logical, outlet end and atmosphere.
5. the hot tank feed system of a kind of intermediate products according to claim 4, which is characterized in that the hot tank volume
5000~30000m3, using vault construction, design normal pressure is 3000 Pa（Table）, -500 Pa of negative pressure（Table）.
6. the hot tank feed system of a kind of intermediate products according to claim 4, which is characterized in that described double to exhale valve be tight
It suddenly releases safety devices, double to exhale valve level pressure value be 1765Pa（Table）, when hot tank deck pressure is higher than 1940Pa（Table）When, it is double that valve is exhaled to open
Outside exhaust is opened, when hot tank deck pressure is less than 1605Pa（Table）When, it is double that valve is exhaled to close, when hot tank deck pressure is less than -294Pa（Table）
When, it is double to exhale valve to open to supplement air into hot tank, prevent hot tank build the pressure or take out it is flat.
7. the hot tank feed system of a kind of intermediate products according to claim 4, which is characterized in that the tank deck of the hot tank is protected
Temperature uses micro-nano thermal insulation board（3mm）+ vacuum forming ceramic beaverboard（60mm）Insulating layer, outer layer coated with hard polyurethane water proof
Layer+metal color steel is protected, and tank skin heat preservation is using the micro-nano thermal insulation board of lining（3mm）+ vacuum forming ceramic beaverboard（180mm）+
Metal color steel is protected, and to ensure that insulating layer hull-skin temperature is less than 50 DEG C, reduces heat loss.
8. the hot tank feed system of a kind of intermediate products according to claim 4, which is characterized in that the hot tank uses nitrogen
Envelope, is carried out automatically controlling with hot tank deck pressure, and isolation air is in direct contact with oil product in tank, avoids the oxygen in air and centre
Oxidation occurs during high-temperature storage and generates colloid or other oxygen carriers for unsaturated hydrocarbons contained in product, and hydrogen is caused to disappear
Consumption increases, catalyst duct blocks and equipment scaling, influences the cycle of operation of downstream unit and the service life of catalyst.
9. the hot tank feed system of a kind of intermediate products according to claim 3, which is characterized in that the Volatile Gas recycling
Unit is the purifying processing device of the light oil and lighter hydrocarbons gas that recycle the moisture, volatilization that are vaporized from hot tank comprising passes through pipeline
The individual calling valve outlet that is sequentially communicated, single breathing valve, anti-detonation type spark arrester, frequency converting induced draft fan, water cooler, three phase separation tank, desulfurization
Tower and lighter hydrocarbons gas takeoff line composition, the three phase separation tank bottom dehydration packet outlet are connected with sewage pump intake, and sewage is by described
Sewage pump is intermittently delivered to acidic water stripping device by sewage output line；The three phase separation pot bottom outlet is pumped with light oil
Entrance is connected, and light oil is intermittently delivered to light oil tank field by light oil pump supercharging by light oil export pipeline；The three-phase
Knockout drum top exit is connected with desulfurizing tower bottom air inlet, and solidifying lighter hydrocarbons gas does not enter from desulfurization tower bottom；The desulfurization
Top of tower outlet is connected to by lighter hydrocarbons gas takeoff line with low pressure gas pipe network, the desulfurizing tower outlet at bottom and lye pump arrival end
Connection, the lye pump discharge divide two-way, first via pipeline to be lye pipeloop, are connected to lye import at the top of desulfurizing tower,
Second road pipeline is alkaline residue output line, is connected to sewage stripping note alkali tank.
10. the hot tank feed system of a kind of intermediate products according to claim 9, which is characterized in that the desulfurizing tower is to fill out
Expect tower, concentration 5-15%（Mass concentration）Sodium hydroxide lye be pressurized by lye pump, desulfurizing tower is delivered to by lye circular route
Top, with from desulfurization tower bottom into lighter hydrocarbons gas in desulfurizing tower counter current contacting, remove sulfide, the lighter hydrocarbons gas after desulfurization passes through
Lighter hydrocarbons gas takeoff line enters low pressure gas pipe network, and the lye extracted out from bottom of tower recycles, and is less than 5% in concentration of lye（Quality is dense
Degree）When, it is pressurized by lye pump, being intermittently delivered to acidic water stripping device by alkaline residue output line is used as note alkali.
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