CN102219184A - Process for preheating raw material of hydrogen production device - Google Patents
Process for preheating raw material of hydrogen production device Download PDFInfo
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- CN102219184A CN102219184A CN2010101448835A CN201010144883A CN102219184A CN 102219184 A CN102219184 A CN 102219184A CN 2010101448835 A CN2010101448835 A CN 2010101448835A CN 201010144883 A CN201010144883 A CN 201010144883A CN 102219184 A CN102219184 A CN 102219184A
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Abstract
The invention discloses a process for preheating raw material of a hydrogen production device. The process comprises the following steps: causing hydrogen production raw material to conduct heat exchange first with medium changing gas, and then with overhot medium pressure steam, preheating the raw material to 350-380 DEG C, then conducting hydrodesulfurization reaction, mixing the overhot medium pressure steam after the temperature reducing with the hydrogen production raw material after hydrodesulfurization, and taking the mixture as the raw material of the hydrogen production device. By using the process, the afterheat of the medium changing gas is utilized fully, the boiler feedwater can not be vaporized, the raw material can be preheated to the needed temperature in an initial working period, and the operation is stable.
Description
Technical field
The invention belongs to the refining of petroleum field, be specifically related to the technology of raw material preheating in a kind of device for producing hydrogen.
Technical background
In recent years, along with the enhancing of people's environmental consciousness, market is to improving constantly that oil quality requires, and simultaneously, crude resources is heaviness more and more, and the highly acid crude oil of high-sulfur inferior proportion in refinery increases gradually.Therefore, variously in the modern refining of petroleum production process face the hydroprocessing technology fast development, driven thereupon the hydrogen demand amount is risen year by year, thereby promoted the develop rapidly of hydrogen producing technology.At present, process for making hydrogen mainly contains: water electrolysis method, ammonia decomposition method, methanol steam conversion method, lighter hydrocarbons steam reforming technology and gasification hydrogen producing technology, wherein the lighter hydrocarbons producing hydrogen from steam conversion has occupied dominant position in plant hydrogen production.
Lighter hydrocarbons steam conversion hydrogen production plant energy consumption height also is the device of heat surplus simultaneously, how to make good use of the device heat, and it is the key of saving energy and reduce the cost that heat is mated mutually.Conventional lighter hydrocarbons steam conversion hydrogen production plant is mainly graded and is formed by boost part, raw material preheating heating-up section, feed purification hydrogenating desulfurization part, water vapor transform portion, transformationreation and heat recovery section, the components of system as directed of steaming and PSA purification portion of raw material compression.Wherein, the raw material preheating heating-up section needs system to provide thermal source that raw material preheating is arrived 350-380 ℃, satisfies the active requirement of feed purification hydrogenating desulfurization partial hydrogenation catalyzer and sweetening agent; The components of system as directed of steaming makes full use of the convection zone flue gas of device for producing hydrogen converter and the heat of converter outlet reforming gas, be provided with in one and press drum, produce the saturated middle pressure steam of 4.2-4.4MPa (G), saturation steam is superheated to 420-440 ℃ through the converter convection zone, superheated vapour divides two portions, and a part is the overheated middle pressure steam of raw material, and it is personal to make the technology raw material, another part is outer defeated steam, and carrying device is to the middle pressure steam pipe network.
Device for producing hydrogen traditional raw material pre-heating technique mainly contains following two kinds of situations:
1) adopt the raw material preheating stove, middle change gas is directly used in the preboiler feedwater.As the technology of introducing in Chinese patent ZL200910118691.0 and periodical " Industrial Catalysis " 2007.15 volumes, this process energy consumption height, need consumption systems fuel gas, and because middle change gas heat surplus, be directly used in the preboiler feedwater, can make oiler feed that the part vaporization has been arranged before entering drum, thereby cause steam quality to descend.
2) adopt an interchanger, by the direct preheating material of middle change gas.As periodical " Shandong petrochemical complex " 2006,34 (3) technologies of introducing, interchanger adopts the vertical disc tubular construction, though this technology has been utilized the middle temperature waste heat (becoming the heat of gas promptly) of device, but go into operation the initial stage at device, because the conversion catalyst activity is good, the depth of conversion height, its remaining CO amount is few, goes out to become the temperature degree in the middle temperature transformation reactor low, and raw material is difficult to be preheating to the temperature of needs, can't satisfy the active requirement of subsequent handling hydrogenation catalyst and sweetening agent, this coil heat exchanger complex structure simultaneously, manufacture difficulty is big, easily leaks.
Therefrom become gas UTILIZATION OF VESIDUAL HEAT IN angle analysis, be not used in preheating material if become the gas heat in the tradition, the steam oiler feed of usefulness of general direct preheating, middle change gas heat makes part oiler feed vaporization, enter drum and carry out carbonated drink separation, cause steam quality to descend, do not vaporize if guarantee oiler feed, then middle change gas UTILIZATION OF VESIDUAL HEAT IN is insufficient, and during moving down into, heat becomes the gas air-cooler, increase power consumption, it is defeated outward to reduce steam simultaneously again, and the energy utilization is very unreasonable.
Summary of the invention
Becoming the gas waste heat in The present invention be directed in the prior art not have shortcoming such as reasonable utilization and a kind of new hydrogen feedstock pre-heating technique is provided, use technology of the present invention not only can make full use of the middle gas waste heat that becomes, and oiler feed is not vaporized, also can be at the initial stage of going into operation with raw material preheating to required temperature, stable operation.
Technical scheme of the present invention is:
1) become the gas preheating in: hydrogen feedstock is through first interchanger, with the heat exchange of middle change gas, raw material after the preheating enters step 2), middle change gas heating boiler feedwater after the cooling, air inlet body separation facilities is isolated product hydrogen afterwards, and the oiler feed after the intensification produces overheated middle pressure steam through drum and converter convection zone.
2) overheated middle pressure steam preheating: from step 1) through in hydrogen feedstock after becoming the gas preheating through second interchanger, with the overheated middle pressure steam heat exchange of part, carry out hydrodesulfurization reaction afterwards, go out the overheated middle pressure steam of second interchanger and mix raw material with hydrogen feedstock after the hydrogenating desulfurization as device for producing hydrogen.
After being preheating to 350～380 ℃, hydrogen feedstock in second interchanger of the present invention enters hydrodesulphurisatioreactors reactors.
Interchanger can adopt conventional interchanger, preferred U type tubular construction interchanger.
Middle change gas described in the present invention is meant the gaseous product of middle temperature transformation reactor.
The present invention adopts two interchanger serial operations, hydrogen feedstock earlier in first interchanger by the preheating of middle change gas, again in second interchanger by overheated middle pressure steam preheating.It compared with prior art has following advantage:
I) with the prior art 1 that adopts raw material preheating stove preheating material) compare, the present invention has cancelled the raw material preheating stove on the one hand, can save the consumption of fuel gas in the refinery, directly bring economic benefit for factory, become gas elder generation preheating hydrogen feedstock in of the present invention on the other hand, the reheat oiler feed can avoid oiler feed that the phenomenon of part vaporization takes place.
II) with interchanger of employing, prior art 2 by the direct preheating material of middle change gas) compares, the present invention adopts two interchanger preheating materials, during utilizing, first interchanger become the gas preheating, second interchanger is used to from the overheated middle pressure steam preheating of the raw material of converter, low as middle change temperature degree, raw material can be preheating to temperature required in second interchanger, can avoid device to go into operation the initial stage like this, because middle change temperature degree is low, make raw material be difficult to be preheating to temperature required shortcoming, thereby guarantee that raw material enters the temperature of hydrogenator, satisfy hydrogenation catalyst and desulfurizer activity requirement, make the desulfurization of raw material effect remarkable, be the length of device, surely, excellent operation is given security.
Advantages such as also to have flow process simple in the present invention in addition, and stable operation is energy-saving and cost-reducing, and benefit is obvious.
Describe the present invention in detail with the drawings and specific embodiments below, but do not limit the scope of the invention.
Accompanying drawing and description of drawings
Figure is the simple process flow diagram of a kind of hydrogen feedstock preheating of the present invention.
Among the figure: 1-first interchanger; 2-second interchanger; The 3-hydrogenator; The 4-desulphurization reactor; The 5-converter; The 6-drum; 7-middle temperature transformation reactor; The 8-feedwater preheater; The 9-oiler feed; The overheated middle pressure steam of 10-; The saturated middle pressure steam of 11-; The defeated outward steam of 12-; The overheated middle pressure steam of 13-raw material.
Embodiment
As shown in the figure, hydrogen feedstock is through raw material first interchanger 1, and with the middle change gas heat exchange that middle temperature transformation reactor 7 produces, the material temperature after the heat exchange reaches 250-280 ℃, and the hydrogen feedstock after the heat exchange advances second interchanger 2.Middle change gas after the cooling is through feedwater preheater 8 heating boilers feedwater 9, air inlet body separation facilities is isolated product hydrogen afterwards, the temperature that the middle temperature that becomes gas satisfies after oiler feed heats up is lower than below the dew point, vaporize when avoiding oiler feed to go drum 6 that middle pressure steam takes place, after oiler feed 9 heats up, produce the saturated middle pressure steam 11 of 4.2-4.4MPa (G) through drum 6, the steam superheating section of saturated middle pressure steam 11 in converter 5 convection zones is superheated to 420-440 ℃ becomes overheated middle pressure steam 10,10 fens two portions of overheated middle pressure steam, a part is advanced second interchanger 2 for the overheated middle pressure steam 13 of raw material, and another part goes out device as outer defeated steam 12.
Hydrogen feedstock after 1 preheating of first interchanger is in second interchanger 2, and with overheated middle pressure steam 13 heat exchange of raw material, hydrogen feedstock is heated to 350-380 ℃, goes hydrogenator 3 and desulphurization reactor 4 to carry out hydrodesulfurization reaction afterwards.The amount of the overheated middle pressure steam 13 of raw material of advancing second interchanger 2 is by the temperature of the hydrogen feedstock that goes out first interchanger 1 and hydrogenator 3 required feeding temperatures decisions.Be mixed as the raw material of device for producing hydrogen through overheated middle pressure steam 13 of second interchanger, 2 cooled raw materials and the hydrogen feedstock after desulphurization reactor 4 desulfurization, through converter 5 convection zones and radiation section, temperature inversion reactor 7 becomes gas in producing in the warp again, and heat exchange separates preparing product hydrogen.
Claims (4)
1. the technology of a device for producing hydrogen raw material preheating is characterized in that comprising the steps:
1) become the gas preheating in: hydrogen feedstock is through first interchanger, with the heat exchange of middle change gas, raw material after the preheating enters step 2), middle change gas heating boiler feedwater after the cooling, air inlet body separation facilities is isolated product hydrogen afterwards, and the oiler feed after the intensification produces overheated middle pressure steam through drum and converter convection zone;
2) overheated middle pressure steam preheating: from step 1) through in hydrogen feedstock after becoming the gas preheating through second interchanger, with the overheated middle pressure steam heat exchange of part, carry out hydrodesulfurization reaction afterwards, go out the overheated middle pressure steam of second interchanger and mix raw material with hydrogen feedstock after the hydrogenating desulfurization as device for producing hydrogen.
2. technology according to claim 1 is characterized in that: enter hydrodesulphurisatioreactors reactors after the hydrogen feedstock in described second interchanger is preheating to 350～380 ℃.
3. technology according to claim 1 is characterized in that: described first interchanger and second interchanger are U type tubular construction interchanger.
4. technology according to claim 1 is characterized in that: the pressure of described overheated middle pressure steam is 4.2-4.4MPa, and temperature is 420-440 ℃.
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| CN2010101448835A CN102219184A (en) | 2010-04-13 | 2010-04-13 | Process for preheating raw material of hydrogen production device |
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| CN2010101448835A CN102219184A (en) | 2010-04-13 | 2010-04-13 | Process for preheating raw material of hydrogen production device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103508418A (en) * | 2012-06-18 | 2014-01-15 | 中国石油化工集团公司 | Start gas heating system in process of hydrogen production from water vapor and heating method |
| CN107998689A (en) * | 2017-12-04 | 2018-05-08 | 大连理工大学 | Become CO in gas acidity lime set in removing2And O2Be thermally integrated rectifying new process |
| 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 (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101602486A (en) * | 2008-12-16 | 2009-12-16 | 山东三维石化工程股份有限公司 | A kind of technology that reclaims heat energy of variable gas in the device for producing hydrogen |
-
2010
- 2010-04-13 CN CN2010101448835A patent/CN102219184A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101602486A (en) * | 2008-12-16 | 2009-12-16 | 山东三维石化工程股份有限公司 | A kind of technology that reclaims heat energy of variable gas in the device for producing hydrogen |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103508418A (en) * | 2012-06-18 | 2014-01-15 | 中国石油化工集团公司 | Start gas heating system in process of hydrogen production from water vapor and heating method |
| CN103508418B (en) * | 2012-06-18 | 2015-08-12 | 中国石油化工集团公司 | Go into operation gas heating system and heating means in water vapour process for making hydrogen |
| CN107998689A (en) * | 2017-12-04 | 2018-05-08 | 大连理工大学 | Become CO in gas acidity lime set in removing2And O2Be thermally integrated rectifying new process |
| 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 |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
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Application publication date: 20111019 |