CN1390778A - Improved energy-saving heat-exchange transfer process for hydrocarbon vapour - Google Patents
Improved energy-saving heat-exchange transfer process for hydrocarbon vapour Download PDFInfo
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- CN1390778A CN1390778A CN02124264A CN02124264A CN1390778A CN 1390778 A CN1390778 A CN 1390778A CN 02124264 A CN02124264 A CN 02124264A CN 02124264 A CN02124264 A CN 02124264A CN 1390778 A CN1390778 A CN 1390778A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
An energy-saving improvement to the heat-exchange convertor technology for hydrocarbon vapour features that a temp-regulating afterheat boiler is additionally used between two-segment convertor and heat-exchange one-segment convertor to control the temp of two-segment converted gas for said heat-exchange convertor in a certain temp. so ensuring the stable running of said heat-exchange convertor and its high-temp pipeline system, elongating service life of equipment and saving energy.
Description
The present invention relates to the improvement technology that a kind of hydrocarbon vapours heat exchange type transforms energy-saving technique, be applicable to that various hydrocarbon vapours heat exchange types transform the technological process of producing synthetic gas.
Auto-thermal reforming process is that the state-of-the-art new energy-saving process of synthetic gas is produced in hydrocarbon steam conversion in the world today.The core of this technology is to utilize the high-temperature technology gas of secondary reformer, for the conversion reaction of hydrocarbons and water vapor in the heat exchange type one-stage converter boiler tube provides heat, thereby realize the autothermal balance or the half autothermal balance of conversion process, reduce the consumption of the hydrocarbons that is used for combustion heat supplying.This energy-saving technique is at first realized industrialization by Britain I.C.I company the 1980s, thereafter, external Byelorussia lattice sieve De-Nol nitrogen synthesis, U.S. Kellogg company, Japanese thousand Dai Tian companies, Denmark TOPS φ E company and domestic one-tenth reach chemico chemical construction corporation, the general engineering development in Chengdu company etc., the Auto-thermal reforming process that succeed in developing different flow processs in succession, differs from one another.Industrialized both at home and abroad heat exchange type conversion system is divided into autothermal balance and half autothermal balance, two big classes.The autothermal equilibrator replaces traditional external-heat one-stage converter with the heat exchange type one-stage converter, hydrocarbons and the required heat of water vapor conversion reaction in the heat exchange type one-stage converter boiler tube, the high-temperature technology gas that is come by secondary reformer provides, shortage of heat terms of settlement partly, be the part hydrocarbons steam reforming of one section conversion of reason to be loaded move on to secondary reformer, add excess air or oxygen-rich air (or pure oxygen) to secondary reformer, thereby keep the autothermal balance of this system.Half autothermal equilibrator solves shortage of heat method partly, be to keep a less traditional external-heat one-stage converter, in parallel with the heat exchange type one-stage converter or connect thereafter, heat exchange type one-stage converter hydrocarbons and water vapor conversion reaction institute heat requirement, the high-temperature technology gas that is come by secondary reformer provides, the external-heat one-stage converter is still supplied with by burning part hydrocarbons, thereby realizes half autothermal balance of this system.Secondary reformer adds the autothermal equilibrator of excess air, at the reforming gas cleaning section PSA device or deep cooling nitrogen rejection facility need be set, to remove excessive N in the reforming gas
2And CO
2Secondary reformer adds the autothermal equilibrator of oxygen-rich air (or pure oxygen), needs supporting PSA air separation (or the empty branch of the deep cooling) device that is provided with, to produce oxygen-rich air (or pure oxygen).Half autothermal equilibrator does not increase the load of two sections conversions, and secondary reformer still only adds the air of technology metering, thereby does not need above-mentioned corollary apparatus.
Facts have proved of industrialization operation; the hydrocarbon vapours Auto-thermal reforming process of different flow processs; all have the unusual effect of the burning of saving with hydrocarbons; but also expose existing technology and be difficult to two shortcomings of taking into account with the steady running of protection device security improving the hydrocarbons depth of conversion; because of the secondary reformer outlet reforming gas temperature drift structure deteriorate that causes of the accidental overtemperature of secondary reformer particularly, become multiple incidents.The start-stop car is frequent, not only causes financial loss to enterprise, and the energy-saving effect of heat exchange type conversion system is had a greatly reduced quality, and has badly influenced applying of this new energy-saving process.
The objective of the invention is by improving technology; overcome the shortcoming of existing Auto-thermal reforming process; solve and improve hydrocarbons depth of conversion and this a pair of contradiction of protection device security steady running; realize the long period safe and stable operation; prolong service life of equipment; give full play to the energy-saving effect of Auto-thermal reforming process, to promote applying of this new energy-saving process.
Inventive concept of the present invention is such:
The contriver further investigation reveals that; the key of protection heat-exchanged reformer and high temperature piping safe and stable operation thereof; be to improve the Auto-thermal reforming process flow process; the target of process modification must be under the prerequisite that satisfies secondary reformer hydrocarbons depth of conversion, controls the temperature of two sections reforming gas of heat exchange type one-stage converter import effectively.
For realizing purpose of the present invention, between secondary reformer and heat exchange type one-stage converter, set up a temperature adjustment waste heat boiler, as the means of two sections reforming gas temperature of control heat exchange type one-stage converter import, the heat of temperature adjustment waste heat boiler is that steam output must be adjustable.This improvement technology can be controlled at certain limit to the temperature of two sections reforming gas that advance the heat exchange type one-stage converter under the prerequisite that does not influence secondary reformer hydrocarbons depth of conversion, the safe and stable operation of protection heat exchange type one-stage converter and high temperature piping thereof.
The technical scheme that hydrocarbon vapours heat exchange type of the present invention transforms the improvement technology of energy-saving technique is constructed as follows: between secondary reformer and heat exchange type one-stage converter, set up a temperature adjustment waste heat boiler.The high-temperature technology gas of secondary reformer outlet is introduced in the temperature adjustment waste heat boiler pipe, after managing outer de-salted water exchange part heat, enters outside the heat exchange type one-stage converter conversion tube again, and the reactant in conversion tube provides heat.
Be provided with the gas bypassing pipe in the temperature adjustment waste heat boiler, regulate the flow of two sections reforming gas of high temperature by bypass tube, in control temperature adjustment waste heat boiler steam output, the temperature of controlling two sections reforming gas of temperature adjustment waste heat boiler outlet effectively is in certain limit.Two sections reforming gas temperature that wherein enter the temperature adjustment waste heat boiler are 850～1050 ℃, and two sections reforming gas temperature that go out the temperature adjustment waste heat boiler are controlled at 750～950 ℃.
The improvement technology that hydrocarbon vapours heat exchange type of the present invention transforms energy-saving technique can be applicable to various hydrocarbon vapours heat exchange types and transforms and produce in the technological process of synthetic gas, comprises heat exchange type excess air autothermal equilibrium conversion process, heat exchange type oxygen-rich air or pure oxygen autothermal equilibrium conversion process, heat-exchanging type parallel half autothermal equilibrium conversion process and the heat exchange type half autothermal equilibrium conversion process of connecting.
Below, narrate technical process of the present invention in conjunction with the accompanying drawings.
Accompanying drawing hydrocarbon vapours heat exchange type transforms the improvement technology generations surface low journey synoptic diagram of energy-saving technique
Wherein: 1---the heat exchange type one-stage converter
2---secondary reformer
3---the temperature adjustment waste heat boiler
Pressure is 0.5～4MPa, be preheated to 400～600 ℃ of temperature, steam/hydrocarbons ratio is that 2.5～3.0 raw material hydrocarbon gas (is represented composition CH
4) with the gas mixture of water vapor, enter in the conversion tube of heat exchange type one-stage converter 1, under the katalysis of interior pipe catalyzer, by means of the external two sections heats that reforming gas provided of conversion tube from temperature adjustment waste heat boiler 3, hydrocarbon gas and water vapor generation conversion reaction and generate H
2, CO and CO
2After reaction proceeds to a certain degree, temperature is that one section reforming gas of 600～800 ℃ leaves heat exchange type one-stage converter 1, enter secondary reformer 2 tops, the oxygen-containing gas (air, oxygen-rich air or pure oxygen) and the fierce turbulence of make up water steam that are 0.4～4MPa with the pressure that adds simultaneously, are preheated to 400～650 ℃ of temperature mix generation H
2With O
2Combustion reactions and emit a large amount of heats, the mixed gas band heat from top to bottom by beds, finishes the degree of depth conversion reaction of hydrocarbon gas under the katalysis of catalyzer.When reaction proceeds to a certain degree is temperature out when reaching 850～1050 ℃, and high-temperature technology gas leaves secondary reformer 2, enters in the pipe of temperature adjustment waste heat boiler 3, carry out heat exchange with the outer de-salted water of pipe after, leave temperature adjustment waste heat boiler 3.Temperature is after 90～180 ℃ de-salted water enters temperature adjustment waste heat boiler 3, the heat of two sections reforming gas of high temperature in the absorption tube, and gasifying is water vapor, enters the heating network of system after carbonated drink is separated.Be provided with the gas bypassing pipe in the temperature adjustment waste heat boiler 3, partly two sections reforming gas of high temperature are through the outlet of the through temperature adjustment waste heat boiler 3 of shortcut pipe, by the flow of regulating by two sections reforming gas of high temperature in the shortcut pipe, can in control temperature adjustment waste heat boiler 3 steam output, control out the temperature of two sections reforming gas of temperature adjustment waste heat boiler 3.From temperature adjustment waste heat boiler 3, temperature is two sections reforming gas of 750～950 ℃, enter outside the conversion tube of heat exchange type one-stage converter 1, with the reactant in the heat transferred conversion tube, after self temperature is reduced to 500～700 ℃, leave heat exchange type one-stage converter 1, follow original technical process then, after the heat exchange cooling, go reforming gas to purify and the post-treatment operation.
The contriver particularly points out, and improves technology generations surface low journey and is applied to different Auto-thermal reforming process, all can obtain same improvement effect:
1. protect heat exchange type one-stage converter and high temperature piping safe and stable operation thereof, prolongation is established
Be equipped with work-ing life and turnaround, reduce start-stop train number number and causality loss, save
Standing charges and running cost.
2. needn't fall because of the operating safety of taking heat exchange type one-stage converter and high temperature piping thereof into account
The depth of conversion of hydrocarbon gas in the low secondary reformer guarantees in two sections reforming gas remaining
CH
4≤ 0.5%, the raw material hydrocarbon gas that reduces unit product consumes, and saves reforming gas
Compression power consumption in purification and the post-treatment.
Above-mentioned improvement effect will make the energy-conservation excellent heat of Auto-thermal reforming process be not fully exerted undoubtedly, promote applying of this new energy-saving process.
Below in conjunction with the production instance of the heat-exchanging type parallel half autothermal equilibrium conversion process after improving, further illustrate content of the present invention.
Embodiment:
Pressure is 1.2MPa, be preheated to 520 ℃, flow is that the Sweet natural gas of 63Kgmol/h and gas mixture (water carbon mol ratio is 2.7) that flow is the water vapor of 170Kg mol/h are divided into two strands, wherein one (account for total amount 45%) enters in the conversion tube of heat exchange type one-stage converter 1, under the katalysis of pipe inner catalyst, by the external two sections heats that reforming gas provides of pipe, CH from temperature adjustment waste heat boiler 3
4With water vapor generation conversion reaction, generate H
2, CO and CO
2, the one section reforming gas temperature that goes out heat exchange type one-stage converter 1 is 680 ℃, CH
4Content reduces to 20%; Another strand (account for total tolerance 55%) enters in the conversion tube of external-heat one-stage converter (not marking in the accompanying drawing), under the katalysis of pipe inner catalyst, is about the heat that the fuel natural gas burning of 18Kgmol/h provides by the pipe external flux, carries out CH
4With the conversion reaction of water vapor, the one section reforming gas temperature that goes out the external-heat one-stage converter is 760 ℃, CH
4Content reduces to 6%.Two strands of one section reforming gas enter secondary reformer 2 tops after merging, and are 1.1MPa with the pressure of having allocated a small amount of water vapor into that adds simultaneously, to be preheated to 500 ℃ of temperature, flow be that the process air of 90Kgmol/h mixes the H in the gas mixture
2With O
2Acutely burn and emit heat, hot gas flow is from top to bottom by beds, one section residue CH that reforming gas is brought into
4Carry out degree of depth conversion reaction with water vapor.
Two sections reforming gas temperature that go out secondary reformer 2 are 950 ℃, remaining CH
4Content＜0.5%, flow is about 6800Kg/h, enters in the pipe of temperature adjustment waste heat boiler 3, with the outer de-salted water heat exchange of pipe.Regulate the flow by the two sections reforming gas of high temperature in the bypass tube, two sections reforming gas temperature that temperature adjustment waste heat boiler 3 is exported are controlled at 860 ℃.Two sections reforming gas from temperature adjustment waste heat boiler 3 enter outside the conversion tube of heat exchange type one-stage converter 1, and after reactant heat exchange in the conversion tube, temperature is reduced to 560 ℃ and left heat exchange type one-stage converter 1.
The reforming gas that goes out heat exchange type one-stage converter 1 after the heat exchange cooling, goes reforming gas to purify and the post-treatment operation again, can be for the ammonia of synthetic about 118Kg mol/h.Temperature adjustment waste heat boiler 3 adding temperature are 140 ℃ de-salted water, behind the part heat through absorbing two sections reforming gas of high temperature, are 191 ℃ saturated vapor but by-product pressure is 1.3MPa, temperature, send into system's heating network.
Claims (5)
1. the improvement technology of a hydrocarbon vapours heat exchange type conversion energy-saving technique is characterized in that setting up a temperature adjustment waste heat boiler between secondary reformer and heat exchange type one-stage converter; The high-temperature technology gas of secondary reformer outlet is introduced in the temperature adjustment waste heat boiler pipe, after managing outer de-salted water exchange part heat, enters outside the heat exchange type one-stage converter conversion tube again, and the reactant in conversion tube provides heat.
2. improvement technology according to claim 1, it is characterized in that being provided with in the temperature adjustment waste heat boiler gas bypassing pipe, regulate the flow of two sections reforming gas of high temperature by bypass tube, in control temperature adjustment waste heat boiler steam output, the temperature of controlling two sections reforming gas of temperature adjustment waste heat boiler outlet effectively is in certain limit.
3. improvement technology according to claim 1, two sections reforming gas temperature that it is characterized in that entering the temperature adjustment waste heat boiler are 850～1050 ℃, two sections reforming gas temperature that go out the temperature adjustment waste heat boiler are controlled at 750～950 ℃.
4. any one of claim 1-3 improved technology and be can be applicable to various hydrocarbon vapours heat exchange types and transform and produce in the technological process of synthetic gas.
5. the described purposes of claim 4, wherein various hydrocarbon vapours heat exchange types transform the technology of producing synthetic gas and comprise heat exchange type excess air autothermal equilibrium conversion process, heat exchange type oxygen-rich air or pure oxygen autothermal equilibrium conversion process, heat-exchanging type parallel half autothermal equilibrium conversion process and the heat exchange type half autothermal equilibrium conversion process of connecting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN02124264A CN1390778A (en) | 2002-07-12 | 2002-07-12 | Improved energy-saving heat-exchange transfer process for hydrocarbon vapour |
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|---|---|---|---|
| CN02124264A CN1390778A (en) | 2002-07-12 | 2002-07-12 | Improved energy-saving heat-exchange transfer process for hydrocarbon vapour |
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| CN1390778A true CN1390778A (en) | 2003-01-15 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100427384C (en) * | 2005-06-28 | 2008-10-22 | 庞玉学 | A method for preparing CO, synthesis gas and methanol by steam reforming of hydrocarbons |
-
2002
- 2002-07-12 CN CN02124264A patent/CN1390778A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100427384C (en) * | 2005-06-28 | 2008-10-22 | 庞玉学 | A method for preparing CO, synthesis gas and methanol by steam reforming of hydrocarbons |
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