CN1060636A - Two-section radial parallel heat exchanging type ammonia synthetic tower - Google Patents
Two-section radial parallel heat exchanging type ammonia synthetic tower Download PDFInfo
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- CN1060636A CN1060636A CN 91111245 CN91111245A CN1060636A CN 1060636 A CN1060636 A CN 1060636A CN 91111245 CN91111245 CN 91111245 CN 91111245 A CN91111245 A CN 91111245A CN 1060636 A CN1060636 A CN 1060636A
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Abstract
The present invention relates to the equipment of a kind of nitrogen and hydrogen synthetic ammonia.This equipment is tower lower gas inlet flow process, and air-flow is radially to pass through first catalyst layer and second catalyst layer; Even in order to control gas distribution, be provided with the inner control barrel structure at first basket and second basket; In order to prevent cold air crossfire between lower columns pipe type heat transfer organ pipe, and the valve jacket structure is set, helps improving the heat transfer efficiency of interchanger.The present invention is applicable on the large-scale synthetic ammonia installation and uses, and also can be used for methyl alcohol synthetic reactor and other reversible solid catalysis reaction units that puts hot gas.
Description
The present invention relates to the equipment of a kind of nitrogen and hydrogen synthetic ammonia.
Ammonia synthesis converter is the key equipment that synthesis ammonia plant is produced, the good and bad throughput that directly influences Bao Chenganchang of its performance, and raw material and moving consumption of being engaged in, and the performance of ammonia synthesis converter depends primarily on the structure of synthetic ammonia tower inner parts.Since the seventies, because world energy sources anxiety, in order to cut down the consumption of energy, the novel ammonia synthesis converter that much is used for Large Scale Synthetic Ammonia Plants is come out one after another, and the S-200 type ammonia synthesis converter of Denmark Tops φ e company for example changes two sections interlayer cold shock formulas of S-100 type ammonia synthesis converter into two sections centres and cools off indirectly, indirect cooled ammonia synthesis converter in the middle of becoming radially, its major advantage is the transformation efficiency height, the ammonia net value height, and pressure drop and energy consumption are low.This is a kind of effect ammonia synthesis converter preferably, existing more application, but, remain in following shortcoming: the cold air of blend stop formula interchanger in the middle of 1, advancing (unstripped gas, down together) needs send into interchanger by tower upper metal flexible pipe, ammonia synthesis converter for high net value, need the more cold air metallic hose of flowing through, then require the metallic hose bore enough big, this just brings the technical barrier of making the heavy caliber metallic hose; 2, air-flow distribution design system is regulated by the nozzle on the tube that distributes outside, air distributor will occupy bigger space like this, thereby reduce the packing factor of catalyst, and when the catalyst bed is too high, regulated with the nozzle on the outer sparger, will be difficult to control air-flow and distribute; 3, radial layer adopts the dividing plate sealing for preventing the gas short circuit, causes the catalyst malfunction in the catalyst envelope, and the catalyst utilization ratio reduces; 4, owing to adopt Stainless Steel Cloth supporting small-particle catalyst, three covers that this structure is introduced in China are that silk screen disruptive accident all appears in the ammonia synthesis converter of raw material with residual oil.
The objective of the invention is to avoid above-mentioned weak point of the prior art and a kind of energy-conservation, low-speed, high net value, catalyst utilization ratio height are provided, do not adopt the two-section radial parallel heat exchanging type ammonia synthetic tower of metallic hose.
Task of the present invention is achieved in that the cold air inlet in tower bottom one side, and following by-pass cold air inlet, main line cold air inlet, synthesis gas outlet all are located on the tower bottom forging.Internals with coaxial setting in the tower are such-first basket from top to bottom, blend stop formula tubular heat exchange in the middle of being provided with in first basket, second basket, lower columns tubular heat exchanger; Riser upper end in center is inserted in the first basket bottom and the middle blend stop formula tubular heat exchange pipe and is communicated, and the second section bed catalyst that runs through second catalyst layer seal, and the lower end is connected with the lower columns tubular heat exchanger.Following by-pass cold air inlet tube, passes first traverse baffle in lower columns tubular heat exchanger top and communicates with the center riser with coaxial insertion lower columns tubular heat exchanger from the forging of tower lower end.
First basket by following several parts (with coaxial, from inside to outside)-middle blend stop formula tubular heat exchange, first section basket inner control tube, first section basket in multihole lamina in the porous tube, first section basket, first section catalyst layer (in the small-particle catalyst is arranged) and first section bed catalyst envelope on top thereof, first section outer multihole lamina of basket, first section outer porous tube of basket.
Second basket by following several parts form (with coaxial, from inside to outside)-center riser, second section basket in multihole lamina, second section catalyst layer (in the small-particle catalyst is arranged) and second section bed catalyst envelope on top thereof, second section outer multihole lamina of basket, second section outer porous tube of basket.The center riser is with coaxial second section bed catalyst envelope of passing the second catalyst layer top.
In order to make in first catalyst layer and second catalyst layer gas distribution even, perforate control on the inner control tube, even in order to regulate the control gas distribution.Because inner control tube periphery is shorter, therefore, when reaching certain flow velocity, controlled more or less freely, more favourable to obtaining higher ammonia net value.
In first catalyst layer neutralizes second catalyst layer, adopt close towards the aperture stainless steel sheet, as the supporting member of small-particle catalyst.
The aperture area of the outer porous tube in first basket and second basket extends to the top, and interior porous tube and inner control tube are limited under the certain height, the difference of altitude at both tops, then constitute the catalyst envelope on catalyst top, it both can prevent the gas short circuit, also can make gas form the diameter of axle, building-up reactions is fully carried out, improve the utilization ratio of catalyst to flowing.
Leave certain space between first basket and second basket, the usefulness of supplied gas circulation leaves certain space between second basket and the lower columns tubular heat exchanger, and supplied gas flows to the interior usefulness of pipe of lower columns tubular heat exchanger.
The lower columns tubular heat exchanger is provided with even numbered blocks traverse baffle-wherein, and half is circular traverse baffle, and second half is a ring baffle plate.In order to prevent cold air along the gap crossfire between traverse baffle and the lower columns tubular heat exchanger shell, and the valve jacket member is set, valve jacket and ring baffle plate driving fit mutually can significantly improve the heat transfer efficiency of lower columns tubular heat exchanger like this.The lower columns tubular heat exchanger is provided with bottom head and the interior bottom head of pipe between pipe, and its effect is that the gas of main line cold air inlet is entered between pipe, and the gas that cold air is entered the mouth enters the annular space of urceolus and inner core.
Description of drawings of the present invention is as follows:
Fig. 1 is structure of the present invention and gas flow synoptic diagram.Among the figure: a cold air inlet, by-pass cold air inlet under the b, c syngas outlet, d main line cold air inlet.1 top cover, 2 urceolus, 3 inner cores, 4 middle blend stop formula tubular heat exchanges, the annular space of 5 urceolus and inner core, bottom head in 6 pipes, bottom head between 7 pipes, 8 forging, 9 times by-pass cold air inlet tubes, 10 lower columns tubular heat exchangers, 11 center riseies, 12 second catalyst layers, 13 first catalyst layers.
Fig. 2 is the structural representation of internals of the present invention.Among the figure: 3 inner cores, 4 middle blend stop formula tubular heat exchanges, bottom head in 6 pipes, bottom head between 7 pipes, 9 times by-pass cold air inlet tubes, 10 lower columns tubular heat exchangers, 11 center riseies, 12 second catalyst layers, 13 first catalyst layers, 14 first sections basket inner control tubes, porous tube in 15 first sections baskets, 16 first sections outer porous tubes of basket, 17 first sections baskets, 18 first sections bed catalyst envelopes, 19 second catalyst layer passages, 20 spaces, 21 second sections bed catalyst envelopes, 22 second sections baskets, 23 second sections outer porous tubes of basket, porous tube in 24 second sections baskets, 25 second sections basket inner control tubes, 26 spaces.
Fig. 3 is the structural representation of lower columns tubular heat exchanger 10 of the present invention.Among the figure: bottom head in 6 pipes, bottom head between 7 pipes, 9 times by-pass cold air inlet tubes, 27 upper tubesheets, 28 traverse baffles, 29 lower tubesheets, 30 lower columns tubular heat exchanger shells, 31 valve jackets, 32 tubulations.
Fig. 4 is the structural representation of first section catalyst pipe of the present invention basket 17.Among the figure: blend stop formula tubular heat exchange in the middle of 4,11 center riseies, 14 first sections basket inner control tubes, porous tube in 15 first sections baskets, 16 first sections outer porous tubes of basket, 33 middle blend stop formula tubular heat exchange urceolus, 34 first sections outer multihole laminas of basket, 35 first sections basket base plates, 36 support, multihole lamina in 37 first sections baskets.
Fig. 5 is the structural representation of second section basket 22 of the present invention.Among the figure: 11 center riseies, 23 second sections outer porous tubes of basket, porous tube in 24 second sections baskets, 25 second sections basket inner control tubes, 38 lock packing letters, 39 second sections outer multihole laminas of basket, 40 second sections basket base plates, multihole lamina in 41 second sections baskets, 42 support.
The present invention is described in further detail below in conjunction with accompanying drawing:
Cold air inlet a is in tower bottom one side, and following by-pass cold air inlet b, main line cold air inlet d, synthesis gas outlet c all are located on the tower bottom forging 8.
Internals with coaxial setting in the tower are such-first section basket 17 from top to bottom, 4, the second sections baskets 22 of blend stop formula tubular heat exchange in the middle of being provided with in first section basket 17, lower columns tubular heat exchanger 10; Riser 11 upper ends in center are inserted in first section basket 17 bottom and middle blend stop formula tubular heat exchange 4 pipes and are communicated, and the second section bed catalyst that runs through second catalyst layer 12 seal 21, and the lower end is connected with lower columns tubular heat exchanger 10.Following by-pass cold air inlet tube 9, passes first traverse baffle 26 in lower columns tubular heat exchanger 10 tops and communicates with center riser 11 with coaxial insertion lower columns tubular heat exchanger 10 from the forging 8 of tower lower end.
In order to make in first catalyst layer 13 and second catalyst layer 12 gas distribution even, perforate control on inner control tube 14,25, even in order to regulate the control gas distribution.Because inner control tube 14,15 peripheries are shorter, so, when reaching certain flow velocity, controlled more or less freely, more effective to obtaining higher ammonia net value.
In first catalyst layer 13 neutralization, second catalyst layer 12, adopt close towards the aperture stainless steel sheet, as the support member of small-particle catalyst.
The aperture area of the outer porous tube 16,23 in first section basket 17 and the second section basket 22 extends to the top, and interior porous tube 15,24 and inner control tube 14,25 are limited under the certain height, its difference of altitude, then constitute the catalyst envelope 18,21 on catalyst layer top, it both can prevent the gas short circuit, also can make gas form the diameter of axle, building-up reactions is fully carried out, improve the utilization ratio of catalyst to flowing.
Leave certain space 20 between in first section basket 17 and the second section basket 22, the usefulness of supplied gas circulation, leave certain space 26 between second section basket 22 and the lower columns tubular heat exchanger 10, supplied gas flows to the interior usefulness of pipe of lower columns tubular heat exchanger 10.
Lower columns tubular heat exchanger 10 is provided with even numbered blocks traverse baffle 28, and wherein half is circular traverse baffle, and second half is a ring baffle plate.In order to prevent cold air along gap crossfire between traverse baffle 28 and the lower columns tubular heat exchanger shell 30, and valve jacket 31 is set, valve jacket 31 and ring baffle plate driving fit mutually can significantly improve the heat transfer efficiency of lower columns tubular heat exchanger 10 like this.Lower columns tubular heat exchanger 10 is provided with between pipe bottom head 6 in bottom head 7 and the pipe, and its effect is that the gas of main line cold air inlet d is entered between pipe, makes the gas of cold air inlet a enter the annular space 5 of urceolus and inner core.
Working condition of the present invention is such: the cold air scale of construction of bay bar formula interchanger 4 accounts for 50～67% of the total cold air scale of construction of tower in entering; be to enter by the cold air of tower bottom one side inlet a; gas by gap 5 following currents of urceolus and inner core on; air-flow as protection tower outer wall; in case tower wall overtemperature is entered in middle blend stop formula interchanger 4 pipes by top again.And enter the gas that accounts for total cold air scale of construction 33～50% between lower columns tubular heat exchanger 10 pipes, d enters by tower bottom main line cold air inlet, through the space 20 that center riser 11 flows between first catalyst layer 13 and second catalyst layer 12, the porous tube 16 that rises then outside first section basket radially enters in the first catalyst layer 13(the small-particle catalyst), pass porous tube 15 and first section basket inner control tube 14 in first section basket, gas ploughs under the second catalyst layer passage 19 along first section basket inner control tube 14 inboard katabatic drainage after between middle blend stop formula interchanger 4 pipes, radially penetrate the outer porous tube 23 of second section basket then, second section outer multihole lamina 39 of basket, enter in the second catalyst layer 12(small-particle catalyst is arranged), gas passes multihole lamina 41 in second basket, second section basket inner control tube 25, enter in lower columns tubular heat exchanger 10 pipes after entering the space 24 between second catalyst layer 12 and the lower columns tubular heat exchanger 10 then, the gas that goes out in the pipe flows out through tower bottom syngas outlet c.According to the technological operation needs, a part of gas warp descends the gas between 9 following current risings of by-pass gas inlet pipe and lower columns tubular heat exchanger 10 pipes to converge and enters center riser 11.
Technic index of the present invention is:
Gasinlet temperature≤140 ℃
Bed hot(test)-spot temperature≤520 ℃
Gas tower exit temperature＜400 ℃
Working pressure≤22MPa
Internals maximum differential pressure 0.3MPa
Medium H in the tower
2, N
2, NH
3, CH
4, Ar.
The present invention has the following advantages compared to existing technology:
1, the cold air entrance of 50～67% cold air of blend stop formula tubular heat exchanger at the bottom of by tower entered in the middle of gas flow of the present invention made and enters. Cold air by the gap following current of urceolus and inner core on, in the middle of being entered by top again in the blend stop formula tubular heat exchanger pipe. (accounting for 33～50% of total air conditioning quantity enters by tower bottom main line cold air entrance and enter cold air between lower columns pipe type heat transfer organ pipe. Above-mentioned this gas flow can guarantee to protect not overtemperature (guaranteeing that tower outer tube inner wall temperature is lower than 200 ℃) of tower outer wall under the condition of high net value, can not adopt metal hose again.
2, adopt interior application cylinder perforate control gas distribution. The Denmark Tops φ e S-200 of company type ammonia convertor, adopt the method for outer distributing barrel and nozzle gas distribution, this structure is not only comparatively complicated, and, very long because of outer distributing barrel periphery, evenly distribute in order to control air-flow, nozzle is arranged inevitable very rare, for not making catalyst layer cause local channel, more than this structure will occupy bigger space. The present invention adopts the method for interior application cylinder perforate control gas distribution, because interior application cylinder periphery is shorter, reaches certain flow rate and is controlled comparatively easily, and the shared space of this structure is less, and is more effective to obtaining higher ammonia net value.
3, adopt the punching stainless sheet steel as the supporting members supports catalyst. China introduces three, and to be embedded with residual oil be that the ammonia convertor of raw material supports catalyst with screen net structure, the accident that stainless steel cloth breaks occurs. Therefore, to make supporting member unreliable for screen net structure. Reliable in order to ensure supporting, the present invention adopts 1～1.5 millimeter hole of the close φ of punching of 0.8～1mm stainless sheet steel as the member of supporting catalyst, all demonstrates superiority than silk screen on welding performance and intensity.
4, adopt catalyst from seal structure. Because gas flow is the diameter of axle to flowing, so, the aperture area of outer porous tube is extended to the top, and make the perforate on the interior application cylinder be limited to certain height, thereby cause top axle Radial Flow structure. Can improve like this catalyst service efficiency at catalyst envelope place. And the Denmark Tops φ e S-200 of company type ammonia convertor adopts the dividing plate sealing, to prevent the gas short circuit, can play a role under the catalyst in the catalyst envelope, and the catalyst utilization rate is lower.
5, employing is with the bottom heat exchanger of valve jacket. The Denmark Tops φ e S-200 of company type ammonia convertor, and domestic and international various ammonia convertor, the bottom heat exchanger is because manufacturing tolerance concerns that cold fluid can be along the gap crossfire between ring baffle plate and the heat exchanger shell inwall between pipe. The present invention adopts sheath structure, can prevent the gas crossfire, thereby significantly improves the heat transfer efficiency of heat exchanger.
The present invention is applicable on the Mass Synthetic Ammonia Unit and uses, and also can be used for methyl alcohol synthetic reactor and other reversible solid catalysis reaction units that puts hot gas.
Claims (3)
1, a kind of two-section radial parallel heat exchanging type ammonia synthetic tower, internals be by first section basket 17,4, the second sections baskets 22 of middle blend stop formula tubular heat exchange, and center riser 11, lower columns tubular heat exchanger 10, following by-pass gas inlet pipe 9 is formed, and it is characterized in that:
(1) is provided with cold air inlet a in tower bottom one side, on tower bottom forging 8, is provided with down by-pass cold air inlet b, syngas outlet c, main line cold air inlet d;
(2) first sections outer porous tube 16 inwalls of basket paste interior porous tube 15 outer walls of outer 34, the first sections baskets of multihole lamina of first section basket of lining and paste multihole lamina 37 in first section basket of lining; Second section outer porous tube 23 inwall of basket pastes interior porous tube 24 outer walls of outer 39, the second sections baskets of multihole lamina of second section basket of lining and pastes multihole lamina 41 in second section basket of lining;
(3) in the lower columns tubular heat exchanger 10 valve jacket 31 is set;
Be provided with in (4) first sections baskets 17 in 14, the second sections baskets 22 of first section basket inner control tube second section basket inner control tube 25 is set.
2, ammonia synthesis converter according to claim 1, it is characterized in that: center riser 11 runs through second section bed catalyst envelope 21 of second catalyst layer 12, communicate in top and middle blend stop formula tubular heat exchange 4 pipes, be connected between bottom and lower columns tubular heat exchanger 10 pipes.
3, ammonia synthesis converter according to claim 1 is characterized in that: lower columns tubular heat exchanger 10 is provided with bottom head 7 and the interior bottom head 6 of pipe between pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 91111245 CN1023995C (en) | 1991-12-03 | 1991-12-03 | Two-section radial parallel heat exchanging type ammonia synthetic tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 91111245 CN1023995C (en) | 1991-12-03 | 1991-12-03 | Two-section radial parallel heat exchanging type ammonia synthetic tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1060636A true CN1060636A (en) | 1992-04-29 |
| CN1023995C CN1023995C (en) | 1994-03-16 |
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ID=4910528
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 91111245 Expired - Fee Related CN1023995C (en) | 1991-12-03 | 1991-12-03 | Two-section radial parallel heat exchanging type ammonia synthetic tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1023995C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105457563A (en) * | 2014-09-09 | 2016-04-06 | 航天长征化学工程股份有限公司 | Isothermal shift reactor with built-in tube bundle |
| CN106629775A (en) * | 2017-01-18 | 2017-05-10 | 山东科技大学 | Multitube-type ultra-low-pressure isothermal ammonia converter |
| CN106698470A (en) * | 2017-01-18 | 2017-05-24 | 山东科技大学 | Helical plate type ultralow-pressure isothermal ammonia synthesizing tower |
-
1991
- 1991-12-03 CN CN 91111245 patent/CN1023995C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105457563A (en) * | 2014-09-09 | 2016-04-06 | 航天长征化学工程股份有限公司 | Isothermal shift reactor with built-in tube bundle |
| CN106629775A (en) * | 2017-01-18 | 2017-05-10 | 山东科技大学 | Multitube-type ultra-low-pressure isothermal ammonia converter |
| CN106698470A (en) * | 2017-01-18 | 2017-05-24 | 山东科技大学 | Helical plate type ultralow-pressure isothermal ammonia synthesizing tower |
| CN106629775B (en) * | 2017-01-18 | 2019-12-06 | 山东科技大学 | tube array type ultra-low pressure isothermal ammonia synthesis tower |
| CN106698470B (en) * | 2017-01-18 | 2019-12-06 | 山东科技大学 | Spiral plate type ultra-low pressure isothermal ammonia synthesis tower |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1023995C (en) | 1994-03-16 |
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Correction item: Co-applicant Correct: East-China Chemical Engineering College|Lanzhou Petro-chemical Design Inst., Chinese Petro-chemical Company. False: East-China Chemical Engineering College Number: 18 Page: 24 Volume: 8 |
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Free format text: CORRECT: CO-APPLICANT; FROM: HUADONG CHEMICAL COLLEGE TO: HUADONG CHEMICAL COLLEGE _ CHINA PETRO-CHEMICAL CORP. LANZHOU PETROLEUM CHEMICAL ENGINEERING DESIGNING INSTITUTE |
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