CN104560161A - Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device - Google Patents

Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device Download PDF

Info

Publication number
CN104560161A
CN104560161A CN201510061224.8A CN201510061224A CN104560161A CN 104560161 A CN104560161 A CN 104560161A CN 201510061224 A CN201510061224 A CN 201510061224A CN 104560161 A CN104560161 A CN 104560161A
Authority
CN
China
Prior art keywords
stage
hydrogenation
pyrolysis gasoline
reactor
pressure steam
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
Application number
CN201510061224.8A
Other languages
Chinese (zh)
Inventor
刘祎婷
印立峰
马伟丽
白玫
何琨
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Engineering Group Co Ltd
Sinopec Shanghai Engineering Co Ltd
Original Assignee
Sinopec Engineering Group Co Ltd
Sinopec Shanghai Engineering Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Sinopec Engineering Group Co Ltd, Sinopec Shanghai Engineering Co Ltd filed Critical Sinopec Engineering Group Co Ltd
Priority to CN201510061224.8A priority Critical patent/CN104560161A/en
Publication of CN104560161A publication Critical patent/CN104560161A/en
Pending legal-status Critical Current

Links

Classifications

    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/405—Limiting CO, NOx or SOx emissions

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention relates to a method for heating materials at the inlet of a second-stage reactor of a pyrolysis gasoline hydrogenation device, for mainly solving the problem of environment pollution when smoke containing NOX and SO2 is discharged to the atmosphere in the prior art. According to the technical scheme of the method for heating the materials at the inlet of the second-stage reactor of the pyrolysis gasoline hydrogenation device, a mixed material of hydrogen and first-stage hydrogenation gasoline fraction is preheated by a second-stage access material heat exchanger and then divided into at least two parts, wherein one part is continuously heated in an ultrahigh-pressure steam heat exchanger and then reacts in the second-stage hydrogenation reactor, and the other part serving as an ultrahigh-pressure steam heat exchanger bypass directly reacts in the second-stage hydrogenation reactor; and the materials reacted in the second-stage hydrogenation reactor are cooled in the second-stage access material heat exchanger and then enter subsequent stations, so that the problem is well solved. The method can be used for heating the materials at the inlet of the second-stage reactor of the pyrolysis gasoline hydrogenation device.

Description

Pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method
Technical field
The present invention relates to a kind of pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method.
Background technology
Pyrolysis gasoline, also known as pyrolysis gasoline.Petroleum chemical industry with lighter hydrocarbons, petroleum naphtha, ordinary pressure diesel, hydrogenation tail oil for raw material, under water vapour existence condition, in the process of Pintsch process preparing ethylene, generating that carbon containing more than five to fractionation does is that the Naphtha solvent of less than 205 DEG C is called pyrolysis gasoline, the a large amount of unsaturated olefin contained in this gasoline and impurity, adopt the method for two-stage catalytic selective hydrogenation to be removed usually.In pyrolysis gasoline hydrogenation device secondary hydrogenation reaction process, two section feedings, except being undertaken except heat exchange heating by two sections of turnover material heat exchangers, also will arrange the temperature in that process furnace is heated to the requirement of second stage reactor hydrogenation reaction further.In combustion, the flue gas to airborne release contains oxynitride NO to process furnace usually xif use the fuel of sulfur-bearing, also will to airborne release sulfide SO 2.Oxynitride NO xwith sulfide SO 2the worldwide environmental problems such as direct or indirect participation depletion of the ozone layer, Greenhouse effect and acid rain, bring very large negative impact to environment, the life of serious threat people and health.
CN201010165197.6 relates to a kind of energy-saving pyrolysis gasoline full-cut hydrogenation method and device, CN201010165188.7 relates to a kind of center fractions of pyrolysis gasoline method of hydrotreating and device, respectively describe the method for hydrotreating of two kinds of pyrolysis gasolines more widely in current industrial application, their invention special emphasis is to reduce the steam of pyrolysis gasoline hydrogenation device and the consumption of water coolant, thus reduces the total energy consumption of pyrolysis gasoline hydrogenation device.CN201320505940.7 relates to a kind of for containing NO xthe selective catalytic reduction denitration device of waste gas, describes a kind of for containing NO xthe selective catalytic reduction denitration device of waste gas, but it is mainly used in the technological process of nitric acid treatment, does not relate in petrochemical complex, and the process furnace especially not in pyrolysis gasoline hydrogenation device reduces NO xand SO 2method.CN200910158011.1 relates to a kind of new and effective low NO xcontrollable flame shape gas burner, it can need to produce according to technique needed for flame profile, be suitable for the tubular oven of various process furnace, particularly petrochemical industry, but just by changing inside heating furnace structure, reach and improve thermo-efficiency and reduce NO xthe object of discharge, does not fundamentally get rid of NO xthe factor produced.CN201210050075.1 relates to a kind of flue gas waste heat recovery desulfurization denitration method and device, this invention can be used for refining of petroleum, petrochemical industry, to occur acid dew piont corrosion and waste heat recovery efficiency problem on the low side for solving when prior art cannot be applied or apply on tubular oven.But this method increase complicacy and the operation easier of integrated artistic flow process, increase project cost and investment, also have certain difficulty for pyrolysis gasoline hydrogenation device.
Thus, prior art arranges process furnace for heating in second-stage hydrogenation reactor entrance material process, exists and contains oxynitride NO to airborne release xwith sulfide SO 2the problem such as flue gas, contaminate environment.The present invention solves this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is that prior art contains NO to airborne release xand SO 2flue gas, contaminate environment problem, a kind of new pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method is provided.The method has and does not contain NO to airborne release xand SO 2flue gas, advantage free from environmental pollution.
For solving the problem, the technical solution used in the present invention is as follows: a kind of pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method, at least two portions are divided into after the mixture of gasoline fraction passes in and out material heat exchanger preheating through two sections after hydrogen and one-stage hydrogenation, a part enters after extra high pressure steam interchanger continues heating and enters second-stage hydrogenation reactor reaction, and another part directly enters second-stage hydrogenation reactor reaction as extra high pressure steam recuperator bypass; The reacted material of second-stage hydrogenation reactor goes to follow-up workshop section after entering the cooling of two sections of turnover material heat exchangers.
In technique scheme, preferably, described second-stage hydrogenation reactor inlet operating temperature is 150 ~ 500 DEG C, and working pressure is 1.5 ~ 5.0MPaG.
In technique scheme, more preferably, described second-stage hydrogenation reactor inlet operating temperature is 220 ~ 300 DEG C, and working pressure is 2.4 ~ 3.0MPaG.
In technique scheme, preferably, described extra high pressure steam operation of heat exchanger temperature is 300 ~ 600 DEG C, and working pressure is 6.0 ~ 16.0MPaG.
In technique scheme, more preferably, described extra high pressure steam operation of heat exchanger temperature is 450 ~ 550 DEG C, and working pressure is 10.0 ~ 14.0MPaG.
In technique scheme, preferably, described extra high pressure steam recuperator bypass pipeline is provided with flow control valve, and after making hydrogen and one-stage hydrogenation by Flow-rate adjustment, the mixture of gasoline fraction reaches the temperature needed for second stage reactor entrance.
In technique scheme, preferably, after after described hydrogen and one-stage hydrogenation, the mixture of gasoline fraction passes in and out material heat exchanger preheating through two sections, by weight, 5 ~ 30% second-stage hydrogenation reactor reaction is directly entered through extra high pressure steam recuperator bypass.
The present invention relates to a kind of pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of environmental protection, in order to prevent will containing oxynitride NO in process furnace combustion processes xwith sulfide SO 2fume emission to air contaminate environment, adopt extra high pressure steam interchanger to replace process furnace heating second stage reactor entrance material, fundamentally cut off oxynitride NO xwith sulfide SO 2the source of discharge, makes whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero, achieve good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1 is the mixture of gasoline fraction after hydrogen and one-stage hydrogenation; 2 is two sections of turnover material heat exchangers; 3 is extra high pressure steam interchanger; 4 is super high pressure steam pipeline; 5 is second-stage hydrogenation reactor; 6 is secondary hydrogenation reaction after product pipeline; 7 is extra high pressure steam recuperator bypass.
As shown in Figure 1, at least two portions are divided into after the mixture (1) of gasoline fraction passes in and out material heat exchanger (2) preheating through two sections after hydrogen and one-stage hydrogenation, a part enters after extra high pressure steam interchanger (3) continues heating and enters second-stage hydrogenation reactor (5) reaction, and another part directly enters second-stage hydrogenation reactor (5) reaction as extra high pressure steam recuperator bypass (7); Second-stage hydrogenation reactor (5) reacted material goes to follow-up workshop section by secondary hydrogenation reaction after product pipeline (6) after entering two sections of turnover material heat exchanger (2) coolings.Extra high pressure steam enters extra high pressure steam interchanger (3) by super high pressure steam pipeline (4).
Fig. 2 is the schematic flow sheet of prior art.
In Fig. 2,1 is the mixture of gasoline fraction after hydrogen and one-stage hydrogenation; 2 is two sections of turnover material heat exchangers; 3 is two sections of process furnace; 4 is fuelgas pipeline; 5 is second-stage hydrogenation reactor; 6 is secondary hydrogenation reaction after product pipeline.
As shown in Figure 2, the mixture (1) of gasoline fraction after hydrogen and one-stage hydrogenation, after two sections of turnover material heat exchanger (2) preheatings, enter two sections of process furnace (3) and be heated to the temperature needed for second stage reactor (5) entrance and enter reactor reaction from second-stage hydrogenation reactor (5) top; Reacted material, after two sections of turnover material heat exchanger (2) coolings, goes to follow-up workshop section by secondary hydrogenation reaction after product pipeline (6).Fuel gas enters two sections of process furnace (3) by fuelgas pipeline (4).
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Extra high pressure steam operation of heat exchanger temperature is 495 DEG C, and working pressure is 12.5MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 10% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 1]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Process furnace chimney height is 50 meters, NO xquantity discharged be 9.1 kgs/hr, SO 2quantity discharged be 29.5 kgs/hr.
[embodiment 2]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 200,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Extra high pressure steam operation of heat exchanger temperature is 495 DEG C, and working pressure is 12.5MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 10% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 2]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 200,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Process furnace chimney height is 30 meters, NO xquantity discharged be 4.2 kgs/hr, SO 2quantity discharged be 14.1 kgs/hr.
[embodiment 3]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 300,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Extra high pressure steam operation of heat exchanger temperature is 495 DEG C, and working pressure is 12.5MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 10% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 3]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 300,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Process furnace chimney height is 40 meters, NO xquantity discharged be 4.9 kgs/hr, SO 2quantity discharged be 16.1 kgs/hr.
[embodiment 4]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 450,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Extra high pressure steam operation of heat exchanger temperature is 495 DEG C, and working pressure is 12.5MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 10% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 4]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 450,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Process furnace chimney height is 40 meters, NO xquantity discharged be 7.3 kgs/hr, SO 2quantity discharged be 24.2 kgs/hr.
[embodiment 5]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 700,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Extra high pressure steam operation of heat exchanger temperature is 495 DEG C, and working pressure is 12.5MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 10% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 5]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 700,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Process furnace chimney height is 50 meters, NO xquantity discharged be 10.6 kgs/hr, SO 2quantity discharged be 34.5 kgs/hr.
[embodiment 6]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 780,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Extra high pressure steam operation of heat exchanger temperature is 495 DEG C, and working pressure is 12.5MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 10% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 6]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 780,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 260 DEG C, and working pressure is 2.7MPaG; Process furnace chimney height is 50 meters, NO xquantity discharged be 11.8 kgs/hr, SO 2quantity discharged be 38.4 kgs/hr.
[embodiment 7]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 150 DEG C, and working pressure is 1.5MPaG; Extra high pressure steam operation of heat exchanger temperature is 300 DEG C, and working pressure is 6.0MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 5% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 7]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 150 DEG C, and working pressure is 1.5MPaG; Process furnace chimney height is 50 meters, NO xquantity discharged be 9.1 kgs/hr, SO 2quantity discharged be 29.5 kgs/hr.
[embodiment 8]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 220 DEG C, and working pressure is 2.4MPaG; Extra high pressure steam operation of heat exchanger temperature is 450 DEG C, and working pressure is 10.0MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 7.5% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 8]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 220 DEG C, and working pressure is 2.4MPaG; Process furnace chimney height is 50 meters, NO xquantity discharged be 9.1 kgs/hr, SO 2quantity discharged be 29.5 kgs/hr.
[embodiment 9]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 300 DEG C, and working pressure is 3.0MPaG; Extra high pressure steam operation of heat exchanger temperature is 550 DEG C, and working pressure is 14.0MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 21.5% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 9]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 300 DEG C, and working pressure is 3.0MPaG; Process furnace chimney height is 50 meters, NO xquantity discharged be 9.1 kgs/hr, SO 2quantity discharged be 29.5 kgs/hr.
[embodiment 10]
On device as shown in Figure 1, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 500 DEG C, and working pressure is 5.0MPaG; Extra high pressure steam operation of heat exchanger temperature is 600 DEG C, and working pressure is 16.0MPaG; Arrange extra high pressure steam recuperator bypass pipeline, the flow of by-pass line accounts for 30% of total flux; After adopting the pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method of a kind of environmental protection of the present invention, whole pyrolysis gasoline hydrogenation device NO xand SO 2quantity discharged be zero.
[comparative example 10]
On device as shown in Figure 2, pyrolysis gasoline hydrogenation device industrial scale is 600,000 tons/year, and second-stage hydrogenation reactor entrance materials handling temperature is 500 DEG C, and working pressure is 5.0MPaG; Process furnace chimney height is 50 meters, NO xquantity discharged be 9.1 kgs/hr, SO 2quantity discharged be 29.5 kgs/hr.

Claims (7)

1. a pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method, at least two portions are divided into after the mixture of gasoline fraction passes in and out material heat exchanger preheating through two sections after hydrogen and one-stage hydrogenation, a part enters after extra high pressure steam interchanger continues heating and enters second-stage hydrogenation reactor reaction, and another part directly enters second-stage hydrogenation reactor reaction as extra high pressure steam recuperator bypass; The reacted material of second-stage hydrogenation reactor goes to follow-up workshop section after entering the cooling of two sections of turnover material heat exchangers.
2. pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method according to claim 1, it is characterized in that described second-stage hydrogenation reactor inlet operating temperature is 150 ~ 500 DEG C, working pressure is 1.5 ~ 5.0MPaG.
3. pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method according to claim 2, it is characterized in that described second-stage hydrogenation reactor inlet operating temperature is 220 ~ 300 DEG C, working pressure is 2.4 ~ 3.0MPaG.
4. pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method according to claim 1, it is characterized in that described extra high pressure steam operation of heat exchanger temperature is 300 ~ 600 DEG C, working pressure is 6.0 ~ 16.0MPaG.
5. pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method according to claim 4, it is characterized in that described extra high pressure steam operation of heat exchanger temperature is 450 ~ 550 DEG C, working pressure is 10.0 ~ 14.0MPaG.
6. pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method according to claim 1, it is characterized in that described extra high pressure steam recuperator bypass pipeline is provided with flow control valve, after making hydrogen and one-stage hydrogenation by Flow-rate adjustment, the mixture of gasoline fraction reaches the temperature needed for second stage reactor entrance.
7. pyrolysis gasoline hydrogenation device second stage reactor entrance heating material method according to claim 1, after after it is characterized in that described hydrogen and one-stage hydrogenation, the mixture of gasoline fraction passes in and out material heat exchanger preheating through two sections, by weight, 5 ~ 30% second-stage hydrogenation reactor reaction is directly entered through extra high pressure steam recuperator bypass.
CN201510061224.8A 2015-02-05 2015-02-05 Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device Pending CN104560161A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201510061224.8A CN104560161A (en) 2015-02-05 2015-02-05 Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201510061224.8A CN104560161A (en) 2015-02-05 2015-02-05 Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device

Publications (1)

Publication Number Publication Date
CN104560161A true CN104560161A (en) 2015-04-29

Family

ID=53077250

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201510061224.8A Pending CN104560161A (en) 2015-02-05 2015-02-05 Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device

Country Status (1)

Country Link
CN (1) CN104560161A (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107937022A (en) * 2017-11-21 2018-04-20 宁波东鼎石化装备有限公司 Pyrolysis gasoline hydrogenation device and method
CN115193340A (en) * 2021-04-09 2022-10-18 中国石化工程建设有限公司 Device and method for heating pyrolysis gasoline hydrogenation reaction feed
CN115594147A (en) * 2021-07-09 2023-01-13 中国石化工程建设有限公司（Cn） Method for preparing hydrogen from methanol and system for preparing hydrogen from methanol

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1287148A (en) * 1999-09-08 2001-03-14 三菱重工业株式会社 Efficient electric power generation method
CN201686667U (en) * 2010-05-07 2010-12-29 中国石油化工集团公司 Cracking gasoline full-fraction hydrogenation device
CN102234541A (en) * 2010-05-07 2011-11-09 中国石油化工集团公司 Energy-saving pyrolysis gasoline full-cut hydrogenation method and device

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1287148A (en) * 1999-09-08 2001-03-14 三菱重工业株式会社 Efficient electric power generation method
US6381943B1 (en) * 1999-09-08 2002-05-07 Mitsubishi Heavy Industries, Inc. High-efficiency power generating method
CN201686667U (en) * 2010-05-07 2010-12-29 中国石油化工集团公司 Cracking gasoline full-fraction hydrogenation device
CN102234541A (en) * 2010-05-07 2011-11-09 中国石油化工集团公司 Energy-saving pyrolysis gasoline full-cut hydrogenation method and device

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
中国石油化工集团公司人事部、中国石油天然气集团公司人事服务中心编: "《汽油加氢装置操作工》", 30 June 2008, article "全馏分加氢工艺流程及特点", pages: 19-24 *
陈砺等编: "《能源概论》", 30 April 2009, article "锅炉节能技术", pages: 232-233 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107937022A (en) * 2017-11-21 2018-04-20 宁波东鼎石化装备有限公司 Pyrolysis gasoline hydrogenation device and method
CN115193340A (en) * 2021-04-09 2022-10-18 中国石化工程建设有限公司 Device and method for heating pyrolysis gasoline hydrogenation reaction feed
CN115594147A (en) * 2021-07-09 2023-01-13 中国石化工程建设有限公司（Cn） Method for preparing hydrogen from methanol and system for preparing hydrogen from methanol

Similar Documents

Publication Publication Date Title
CN108138591B (en) Recovery and reuse of waste energy in industrial plants
CN101659400B (en) Catalyst combination process of sulfur recovering device
CN100544807C (en) The method of a kind of sulphur recovery and exhaust gas processing device and sulphur recovery thereof and vent gas treatment
CN103822217B (en) A kind of sour gas pretreatment technology
CN102910593B (en) System and method for treating waste acid gas
EP3433208B1 (en) Claus unit treatment of shutdown tail gas
CN202336287U (en) Integrated treatment system of organic waste gases of refining company
CN105327599B (en) The processing method of molten sulfur degasification exhaust gas
CN102285729A (en) High-temperature wet-oxidation treatment method for waste alkali liquid
CN104560161A (en) Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device
CA2994281C (en) Systems and methods for improved sulfur recovery from claus process tail gas
CN210973883U (en) Sulfur recovery device is blown in circulation
CN104119946B (en) A kind of catalytic cracking flue gas desulfurization and Acidic Gas Treating technique
CN102000504A (en) SCR denitration device for flue gas of glass furnace
CN205717250U (en) A kind of asphalt smoke gas purifying incinerator
CN104548900A (en) Process device of coke oven fume denitrification, desulfuration and reheating system
CN201031142Y (en) Sulfur recovery and exhaust gas treating device of reheat furnace hydrogen making
CN102395658A (en) High pressure revamp of low pressure distillate hydrotreating process units
CN104828783B (en) A kind of method and device for improving sour gas Sulphuric acid device Acidic Gas Treating amount
CN204365119U (en) A kind of coke oven flue gas denitration desulfurization and reheat system process unit
CN202864918U (en) Waste gas treatment system of acid gas
CN105983331B (en) Industrial sulfur-containing tail gas sulfur removal technology
CN103566730B (en) The sulphur removal produced in process sulfur recovery facility shut-down process purges the method for tail gas
CN105318342B (en) A kind for the treatment of process of industrial smoke
CN210544391U (en) Device for treating pressure swing adsorption decarbonization exhaust gas by catalytic oxidation

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into 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: 20150429