阅读说明：本技术 一体式氨合成热回收设备及氨合成热回收工艺 (Integral type ammonia synthesis heat recovery equipment and ammonia synthesis heat recovering process ) 是由 卢健 王雪林 于 2019-09-20 设计创作，主要内容包括：本发明公开了一体式氨合成热回收设备,包括相互连接的第一列管换热器和第二列管换热器,第一列管换热器具有过热蒸汽出口和回气口；第二列管换热器分为蒸汽发生段和预热段；第二列管换热器的管程连通第一列管换热器的管程；第二列管换热器的壳程与第一列管换热的壳程不相连通；在第二列管换热器的上方设置有连通蒸汽发生段的汽包,汽包连通第一列管换热器的回气口。采用上述设备的氨合成热回收工艺,第二换热器内的水进入到汽包内,产生饱和蒸汽,饱和蒸汽进入到第一换热器内生产过热蒸汽。本申请在具有低制造成本的基础上,保证了设备的耐腐蚀性。利用本设备可以生产热焓较高的过热蒸汽。(The invention discloses integral type ammonia synthesis heat recovery equipment, including the first tubular heat exchanger interconnected and the second tubular heat exchanger, the first tubular heat exchanger has superheated steam outlet and gas returning port；Second tubular heat exchanger is divided into steam generation section and preheating section；The tube side of second tubular heat exchanger is connected to the tube side of the first tubular heat exchanger；The shell side that the shell side of second tubular heat exchanger exchanges heat with the first tubulation is not attached to lead to；The drum of connection steam generation section is provided with above the second tubular heat exchanger, drum is connected to the gas returning port of the first tubular heat exchanger.Using the ammonia synthesis heat recovering process of above equipment, the water in the second heat exchanger is entered in drum, generates saturated vapor, and saturated vapor, which enters, produces superheated steam in First Heat Exchanger.The application ensure that the corrosion resistance of equipment on the basis of with low manufacturing cost.The higher superheated steam of heat content can be produced using this equipment.)

1. integral type ammonia synthesis heat recovery equipment, which is characterized in that including the first tubular heat exchanger and the second tubular heat exchanger, In first tubular heat exchanger include the first shell extended along first axle direction and what is be arranged in the first shell first change The opposite both ends of heat pipe, first shell are respectively formed as the first front end and the first rear end, are equipped with first in the first front end Front tube sheet is equipped with the first back tube sheet in the first rear end, the first heat exchanger tube both ends be respectively and fixedly installed to the first front tube sheet and On first back tube sheet；

First front end of the first shell is provided with reaction gas inlet portion, which has reaction gas inlet chamber, connects Lead to the reaction gas inlet pipe of the reaction gas inlet chamber, which is connected to the tube side of the first tubular heat exchanger；First Rear end is provided with first connecting portion；

Superheated steam outlet and gas returning port are provided on the first shell of the first tubular heat exchanger, superheated steam is exported compared with return-air The first front end of mouth distance is closer；

Second tubular heat exchanger includes along the second housing that second axis direction extends and second in the setting second housing The opposite both ends of heat exchanger tube, the second housing are respectively formed as the second front end and the second rear end, are equipped in the second front end Two front tube sheets are equipped with the second back tube sheet in the second rear end, which is respectively and fixedly installed to the second front tube sheet On the second back tube sheet；

Along second axis direction, which is divided into steam generation section and preheating section, and steam generation section is located towards The side of second front tube sheet；Second front end of the second tubular heat exchanger is provided with second connecting portion, is provided in the second rear end Reaction gas outlet portion, the reaction gas outlet which has reaction gas outlet plenum, is connected to the reaction gas outlet plenum, should Reaction gas outlet plenum is connected to the tube side of the second tubular heat exchanger；

The second connecting portion is connected with first connecting portion, and the tube side of the second tubular heat exchanger is made to be connected to the first tubular heat exchanger Tube side；The shell side that the shell side of second tubular heat exchanger exchanges heat with the first tubulation is not attached to lead to；

It is provided with drum above the second tubular heat exchanger, which is connected to the second tubular heat exchanger with down-comer through tedge Steam generation section shell side；Steam (vapor) outlet is provided at the top of drum, which is connected to returning for the first tubular heat exchanger Port；

Be provided on the shell corresponding to the preheating section of the second tubular heat exchanger connection the second tubular heat exchanger shell side into The mouth of a river.

2. integral type ammonia synthesis heat recovery equipment according to claim 1, which is characterized in that in first connecting portion and second In interconnecting piece one of both, at least one is formed with a reaction gas overcurrent chamber, the tube side of the first tubular heat exchanger and the second tubulation The tube side of heat exchanger is connected to through the reaction gas overcurrent chamber.

3. integral type ammonia synthesis heat recovery equipment according to claim 2, which is characterized in that

The first connecting portion includes the first rear cylinder body and the first rear flange to link together, which is connected to first Extend on back tube sheet and towards the direction away from the first shell, the inner cavity of first rear cylinder body is formed as the reaction gas overcurrent chamber； Or

The second connecting portion includes the second conveyor front barrel and the second forward flange to link together, which is connected to second Extend on front tube sheet and towards the direction away from second housing, the inner cavity of second conveyor front barrel is formed as the reaction gas overcurrent chamber； Or

The first connecting portion includes the first rear cylinder body and the first rear flange to link together, which is connected to first Extend on back tube sheet and towards the direction away from the first shell；The second connecting portion include the second conveyor front barrel for linking together and Second forward flange, second conveyor front barrel are connected on the second front tube sheet and extend towards the direction away from second housing；This is after first The inner cavity of cylinder and the inner cavity of the second conveyor front barrel are collectively formed as the reaction gas overcurrent chamber.

4. integral type ammonia synthesis heat recovery equipment according to claim 3, which is characterized in that

There is S32168 overlay cladding on the inner wall of first rear cylinder body；

There is S32168 overlay cladding on the inner wall of second conveyor front barrel.

5. integral type ammonia synthesis heat recovery equipment according to claim 1, which is characterized in that

Reaction gas inlet portion includes the first conveyor front barrel and drive end bearing bracket, and one end of first conveyor front barrel is connected on the first front tube sheet, The drive end bearing bracket hermetically covers the other end for being located at first conveyor front barrel, and reaction gas inlet pipe is connected to the one of first conveyor front barrel Side；The space of first conveyor front barrel, drive end bearing bracket and the first front tube sheet institute corral is formed as reaction gas inlet chamber；

There is S32168 overlay cladding on the inner wall of first conveyor front barrel and the inner wall of reaction gas inlet pipe；

First front tube sheet has Inconel690 alloy welding deposit layer away from the side of the first back tube sheet.

6. integral type ammonia synthesis heat recovery equipment according to claim 1, which is characterized in that

The side away from the first front tube sheet of first back tube sheet has Inconel690 alloy welding deposit layer；

The side away from the second back tube sheet of second front tube sheet has Inconel690 alloy welding deposit layer.

7. integral type ammonia synthesis heat recovery equipment according to claim 1, which is characterized in that

Second heat exchanger tube includes the first pipeline section and the second pipeline section welded together, which is welded on the second front tube sheet On；The material of first pipeline section is ALLOY690, and the material of the second pipeline section is 15CrMo；

The material of first heat exchanger tube is ALLOY690.

8. integral type ammonia synthesis heat recovery equipment according to claim 1, which is characterized in that

It is tightly connected between first connecting portion and second connecting portion using omega.

9. a kind of ammonia synthesis heat recovering process, which is characterized in that use the described in any item ammonia synthesis recuperations of heat of claim 1-8 Equipment, including following process:

(1) supplement water is entered the shell side of the second tubular heat exchanger by water inlet, is then entered in drum through tedge, part Moisture evaporates to form saturated vapor, which is entered the shell side of the first tubular heat exchanger by gas returning port, is formed after heat absorption Superheated steam simultaneously exports discharge by superheated steam；

Part water body in drum returns to the shell side of the second tubular heat exchanger through down-comer, persistently adds to the water body in drum Heat；

(2) ammonia synthesis gas enters reaction gas inlet portion by reaction gas inlet pipe, subsequently into successively pass through the first heat exchanger tube and The reaction gas of second heat exchanger tube, last reacted gas outlet portion exports discharge, into next procedure.

10. ammonia synthesis heat recovering process according to claim 9, which is characterized in that the pressure of saturated vapor be 4.0 ± 0.1MPa, the pressure of superheated steam are 3.8 ± 0.1MPa, and the temperature of superheated steam is 420 ± 10 DEG C；

Temperature of the ammonia synthesis gas in reaction gas inlet portion is 445 ± 5 DEG C, and temperature is reduced to after entering the second heat exchanger 410 ± 5 DEG C, the discharge temperature in reaction gas outlet is 220 ± 5 DEG C.

Technical field

The present invention relates to obtain thermal energy recycling and technique in ammonia synthesis industry, and in particular to a kind of integral type ammonia synthesis recuperation of heat Equipment and ammonia synthesis heat recovering process.

Background technique

Sufficiently to recycle the reaction heat in ammonia synthesis technology, various heat-exchanger rigs are developed, waste heat boiler is wherein A major class, current waste heat boiler heats soft water using single heat exchanger, substantially based on through type with life The saturated vapor for producing different grades, since the temperature of ammonia synthesis gas is higher, is needed using high-grade as other process steams Material makes heat exchange equipment, so that the manufacturing cost of heat exchange equipment is high.And when entering heat exchanger due to ammonia synthesis gas Temperature it is higher, keep the hydrogen-type corrosion of the inlet part of heat exchanger more serious, to guarantee safety in production, need using higher corrosion resistant The pipeline of erosion ability reduce the cost of heat exchanger can not.

In addition, saturated vapor can only be produced due to using single heat exchanger, the grade of steam, and ammino are not only influenced Also higher at the discharge temperature of gas, thermal energy recovering effect is ideal not to the utmost.

Summary of the invention

It is an object of the invention to overcome drawbacks described above, the application first proposed integral type ammonia synthesis heat recovery equipment, It includes the first tubular heat exchanger and the second tubular heat exchanger, and wherein first tubular heat exchanger includes prolonging along first axle direction The first shell stretched and the first heat exchanger tube being arranged in the first shell, the opposite both ends of first shell are respectively formed as the One front end and the first rear end, are equipped with the first front tube sheet in the first front end, are equipped with the first back tube sheet in the first rear end, this first Heat exchanger tube both ends are respectively and fixedly installed on the first front tube sheet and the first back tube sheet；

First front end of the first shell is provided with reaction gas inlet portion, which has reaction gas inlet Chamber, the reaction gas inlet pipe for being connected to the reaction gas inlet chamber, the reaction gas inlet chamber are connected to the tube side of the first tubular heat exchanger；In First rear end is provided with first connecting portion；

Be provided on the first shell of the first tubular heat exchanger superheated steam outlet and gas returning port, superheated steam outlet compared with The first front end of gas returning port distance is closer；

Second tubular heat exchanger includes along the second housing that second axis direction extends and being arranged in the second housing The opposite both ends of second heat exchanger tube, the second housing are respectively formed as the second front end and the second rear end, install in the second front end There is the second front tube sheet, the second back tube sheet is installed in the second rear end, before which is respectively and fixedly installed to second On tube sheet and the second back tube sheet；

Along second axis direction, which is divided into steam generation section and preheating section, and steam generation section is located at Towards the side of the second front tube sheet；Second front end of the second tubular heat exchanger is provided with second connecting portion, is set in the second rear end It is equipped with reaction gas outlet portion, which has reaction gas outlet plenum, the reaction gas that is connected to the reaction gas outlet plenum goes out Mouthful, which is connected to the tube side of the second tubular heat exchanger；

The second connecting portion is connected with first connecting portion, and the tube side of the second tubular heat exchanger is made to be connected to the heat exchange of the first tubulation The tube side of device；The shell side that the shell side of second tubular heat exchanger exchanges heat with the first tubulation is not attached to lead to；

It is provided with drum above the second tubular heat exchanger, which is connected to the second tubulation with down-comer through tedge and changes The shell side of the steam generation section of hot device；Steam (vapor) outlet is provided at the top of drum, which is connected to the first tubular heat exchanger Gas returning port；

The shell side of the second tubular heat exchanger of connection is provided on the shell corresponding to the preheating section of the second tubular heat exchanger Water inlet.

It is preferably tightly connected using omega between first connecting portion and second connecting portion.

At present in ammonia synthesis gas heat recovery equipment, it is one whole that more mature mode, which is by drum and design of heat exchanger, Body, or use single heat exchanger.

In this application, heat exchanger is using the two-stage heat exchange including the first tubular heat exchanger and the second tubular heat exchanger Device, but the second tubular heat exchanger is divided into steam generation section and preheating section using pipe joint, the application uses multiple combinations Mode makes the first tubular heat exchanger be in high-temperature area, and the second tubular heat exchanger is made to be in low-temperature region.Due to by the prior art In single-stage heat exchanger be divided into the first, second two tubular heat exchangers, can the temperature according to locating for two heat exchangers different shapes State manufactures two tubular heat exchangers using different materials respectively, is guaranteeing that it is roughly the same that equipment has at different temperatures Resistant to hydrogen lose ability while, to be effectively reduced the manufacturing cost of equipment.

In the application, steam generation section and preheating section are designed as a tubular heat exchanger, can not only reduce equipment Total quantity is also reduced when steam generation section and preheating section are divided into two heat exchangers, and brought fluid hose hinders increased disadvantage End.

In the application, the drum of separate type is set, is arranged drum according to the concrete condition at scene, Er Qieshe After setting individual drum, since the corrosion that drum is received is less, it can cause to avoid the corrosion due to heat exchanger pair The destruction of drum.Even if also significantly reducing the replacement number to drum substantially in more exchange device.

When producing hot vapour using the application, the water body in drum can carry out between drum and the second tubular heat exchanger Natural Circulation, without being driven using additional kinetic pump.

To guarantee that ammonia synthesis gas is smoothly entered by the first tubular heat exchanger to the second tubular heat exchanger, in first connecting portion In second connecting portion one of both, at least one is formed with a reaction gas overcurrent chamber, the tube side of the first tubular heat exchanger and The tube side of two tubular heat exchangers is connected to through the reaction gas overcurrent chamber.

Specifically, which includes the first rear cylinder body and the first rear flange to link together, the cylinder after first Body is connected on the first back tube sheet and extends towards the direction away from the first shell, and the inner cavity of first rear cylinder body is formed as described Reaction gas overcurrent chamber；Or

The second connecting portion includes the second conveyor front barrel and the second forward flange to link together, which is connected to Extend on second front tube sheet and towards the direction away from second housing, the inner cavity of second conveyor front barrel is formed as the reaction gas mistake Flow chamber；Or

The first connecting portion includes the first rear cylinder body and the first rear flange to link together, which is connected to Extend on first back tube sheet and towards the direction away from the first shell；The second connecting portion includes the second placket to link together Body and the second forward flange, second conveyor front barrel are connected on the second front tube sheet and extend towards the direction away from second housing；This The inner cavity of one rear cylinder body and the inner cavity of the second conveyor front barrel are collectively formed as the reaction gas overcurrent chamber.

After one reaction gas overcurrent chamber is set, make the mixing that an ammonia synthesis gas is formed between the first tubulation and the second tubulation On the one hand chamber, the mixing chamber can make the equalizing temperature of the ammonia synthesis gas flowed out from the first tubulation, be conducive to improve secondary series On the other hand the heat exchange efficiency of heat exchange of heat pipe is avoided due to, since distance is very little, and causing between the first tubulation and the second tubulation Ammonia synthesis gas generates turbulent flow between the first tubulation and the second tubulation, consumes energy, while generating larger vibration, influences equipment Safe handling.

Further, for guarantee high temperature under, equipment to ammonia synthesis gas have preferable anti-corrosion capability, the first rear cylinder body it is interior There is S32168 overlay cladding on wall；There is S32168 overlay cladding on the inner wall of second conveyor front barrel.

It is preferred that the first rear cylinder body and the second conveyor front barrel be using 12Cr2mo1 steel alloy pipe fitting as substrate, and closed in 12Cr2mo1 On the inner wall of golden steel pipe fitting construct S32168 overlay cladding and formed.

After stainless steel weld overlays are set, the anti-corrosion capability of equipment can be effectively improved, the service life of equipment is extended.

Further, to improve the anti-corrosion capability of equipment at high temperature, reaction gas inlet portion includes the first conveyor front barrel with before End cap, one end of first conveyor front barrel are connected on the first front tube sheet, which hermetically covers and be located at first conveyor front barrel The other end, reaction gas inlet pipe are connected to the side of first conveyor front barrel；First conveyor front barrel, drive end bearing bracket and the first front tube sheet are enclosed The space enclosed is formed as reaction gas inlet chamber；

There is S32168 overlay cladding on the inner wall of first conveyor front barrel and the inner wall of reaction gas inlet pipe；First front tube backboard Side from the first back tube sheet has Inconel690 alloy welding deposit layer.Preferably using Europe rice between first conveyor front barrel and drive end bearing bracket Gal is tightly connected.

Preferably, first conveyor front barrel and reaction gas inlet pipe be using 12Cr2mo1 steel alloy pipe fitting as substrate, and On the inner wall of 12Cr2mo1 steel alloy pipe fitting construct S32168 overlay cladding and formed.

It is preferred that the first front tube sheet is using 12Cr2mo1 alloy steel casting as substrate, and applied on the 12Cr2mo1 alloy steel casting Work Inconel690 alloy welding deposit layer and formed.

The application overlay cladding different according to different structural devices, since the first front tube sheet will bear more complicated answer Power, using Inconel690 alloy welding deposit layer, to guarantee that the first front tube sheet has excellent stress corrosion resistant ability.Due to first Conveyor front barrel and reaction gas inlet pipe have cylindric structure, anti-pressure ability with higher itself, therefore slightly lower using cost S32168 overlay cladding, while including has the ability of equipment stress corrosion resistant with higher, to drop to the maximum extent The manufacturing cost of low equipment.

It further, is the resistance to corrosion for improving equipment, the side away from the first front tube sheet of the first back tube sheet has Inconel690 alloy welding deposit layer；The side away from the second back tube sheet of second front tube sheet has Inconel690 alloy welding deposit Layer.

It is preferred that the first back tube sheet and the second front tube sheet be using 12Cr2mo1 alloy steel casting as substrate, and in the 12Cr2mo1 On alloy steel casting construct Inconel690 alloy welding deposit layer and formed.

Further, the second heat exchanger tube includes the first pipeline section and the second pipeline section welded together, which is welded on On second front tube sheet；The material of first pipeline section is ALLOY690, and the material of the second pipeline section is 15CrMo；The material of first heat exchanger tube Material is ALLOY690.That is the material of the first heat exchanger tube all uses ALLOY690 to make.

Second tubulation is spliced by the pipe of different materials, wherein being used close to one end of the first tubular heat exchanger ALLOY690, to guarantee at high operating temperatures, the resistance to corrosion of the second tubulation, and the second pipeline section is used into 15CrMo tubes of material Road, using low price 15CrMo pipeline, has been able to satisfy anticorrosive since in the area, temperature has been reduced significantly It is required that.The anti-corrosion ability in each region is set to reach one uniformly using different anti-corrosion materials using according to different heat affected zones Level, on the basis of making full use of the good resistance to hydrogen attack ability of each material, also reduce equipment construction cost.

, to postwelding, weld seam is polished by the first pipeline section and the second pipeline section, keeps the smooth of secondary series pipe outer wall.First pipe The length of section is substantially controlled to be preferred in 450-700mm.Keep the smooth of secondary series pipe outer wall, it is possible to reduce to water body flow Interference, while guaranteeing in temperature change, which still is able to provide enough deformations, to reduce the aggregation of internal stress.

Secondly, the application also provides a kind of ammonia synthesis heat recovering process, above-mentioned any one ammonia synthesis recuperation of heat is used Equipment carries out, and specifically includes following process:

(1) supplement water is entered the shell side of the second tubular heat exchanger by water inlet, is then entered in drum through tedge, Partial moisture evaporates to form saturated vapor, which is entered the shell side of the first tubular heat exchanger by gas returning port, after heat absorption It forms superheated steam and is exported by superheated steam and is discharged；

Part water body in drum returns to the shell side of the second tubular heat exchanger through down-comer, continues to the water body in drum Heating；

(2) ammonia synthesis gas enters reaction gas inlet portion by reaction gas inlet pipe, exchanges heat subsequently into successively passing through first The reaction gas of pipe and the second heat exchanger tube, last reacted gas outlet portion exports discharge, into next procedure.

Preferably, the pressure of saturated vapor is 4.0 ± 0.1MPa, and the pressure of superheated steam is 3.8 ± 0.1MPa, and overheat is steamed The temperature of vapour is 420 ± 10 DEG C；

Temperature of the ammonia synthesis gas in reaction gas inlet portion is 445 ± 5 DEG C, and temperature reduces after entering the second heat exchanger To 410 ± 5 DEG C, the discharge temperature in reaction gas outlet is 220 ± 5 DEG C.

High-grade superheated steam can also be generated while improving thermal energy recycling using above-mentioned recovery process, is it His process requirement provides the selection of more steam use aspects.It is steamed it is of course also possible to directly lead out saturation at the top of drum Vapour, for other production and applications.

Detailed description of the invention:

Fig. 1 is the structure diagram of one embodiment of the invention.

Fig. 2 be in Fig. 1 A-A to view.

Fig. 3 is the enlarged drawing of part B in Fig. 1.

Fig. 4 is the enlarged drawing of C portion in Fig. 1.

Fig. 5 is the enlarged drawing of the part D in Fig. 4.

Specific embodiment:

Integral type ammonia synthesis heat recovery equipment is illustrated first below.

Fig. 1 and Fig. 2 are please referred to, the arrow M that appropriate location is marked in Fig. 1 is axis direction, in this embodiment, first Axis and the extending direction of second axis are identical as axis direction M.

The ammonia synthesis heat recovery equipment includes the first tubular heat exchanger 10 and the second tubular heat exchanger 20.

Wherein first tubular heat exchanger 10 includes the first shell 11 extended along first axle direction and is arranged first Several first heat exchanger tubes 12 in shell.The opposite both ends of first shell are respectively formed as the first front end 118 and first Rear end 119, is equipped with the first front tube sheet 115 in the first front end 118, is equipped with the first back tube sheet 116 in the first rear end 119, should First heat exchanger tube, 11 both ends are respectively and fixedly installed on the first front tube sheet 115 and the first back tube sheet 116.

First front end 118 of the first shell 11 is provided with reaction gas inlet portion, which has reaction gas Snout cavity 131, the reaction gas inlet pipe 132 for being connected to the reaction gas inlet chamber, the reaction gas inlet chamber 131 are connected to the first tubulation and change The tube side of hot device 10.

Reaction gas inlet portion includes the first conveyor front barrel 13 and drive end bearing bracket 16, and one end of first conveyor front barrel 13 is connected to first On front tube sheet 115, which hermetically covers the other end for being located at first conveyor front barrel 13 using the first bolt 161, reaction Gas inlet pipe 132 is connected to the side of first conveyor front barrel 13.Omega is used between drive end bearing bracket 16 and the first conveyor front barrel 13 It is tightly connected.The space of first conveyor front barrel 13, drive end bearing bracket 16 and first 115 corrals of front tube sheet is formed as reaction gas inlet chamber 131。

Superheated steam outlet 113 and gas returning port 111, overheat are provided on the first shell 11 of the first tubular heat exchanger 10 The setting of steam (vapor) outlet 113 is relatively returned in the first front end 118, the setting of gas returning port 111 in the first rear end 119, i.e. superheated steam outlet 113 111 the first front end of distance of port is closer.

Second tubular heat exchanger 20 includes the second housing 21 and the setting second housing extended along second axis direction Several second heat exchanger tubes 22 in 21, the opposite both ends of the second housing 21 are respectively formed as the second front end 218 and second Rear end 219, is equipped with the second front tube sheet 34 in the second front end 218, is equipped with the second back tube sheet 35 in the second rear end 219, this Two heat exchanger tubes, 22 both ends are respectively and fixedly installed on the second front tube sheet 34 and the second back tube sheet 35.

Along second axis direction, which is divided into steam generation section 200 and preheating section 300, in Fig. 1, Steam generation section 200 and preheating section 300 are substantially separated along dotted line 400.Steam generation section 300 is located towards the second front tube sheet 34 Side.Second front end of the second tubular heat exchanger is provided with second connecting portion, the second rear end is provided with reaction gas outlet portion, The reaction gas outlet 332 that the reaction gas outlet portion has reaction gas outlet plenum 331, is connected to the reaction gas outlet plenum 331, the reaction Gas outlet plenum 331 is connected to the tube side of the second tubular heat exchanger 20.

To avoid damaging second housing 21 due to temperature change, in the present embodiment, preheating section 300 pair Metal connecting hose 37 is provided on the second housing answered.

In the present embodiment, reaction gas inlet portion include the second rear cylinder body 33 and rear end cap 36, the one of second rear cylinder body 33 End is connected on the second back tube sheet 35, which is hermetically covered using the second bolt 361 and be located at second rear cylinder body 33 The other end, reaction gas outlet 332 are formed in the side of second rear cylinder body 33.

It is tightly connected between rear end cap 36 and the second rear cylinder body 33 using omega.Second rear cylinder body 33, rear end cap 36 Be formed as reaction gas outlet plenum 331 with the space of second 35 corrals of back tube sheet.

First rear end is provided with first connecting portion, which is connected with second connecting portion, makes the second tubulation The tube side of heat exchanger is connected to the tube side of the first tubular heat exchanger；The shell side of the shell side of second tubular heat exchanger and the heat exchange of the first tubulation It is not attached to lead to.

In the present embodiment, which includes the first rear cylinder body 14 and the first rear flange 81 to link together, First rear cylinder body 14 is connected on the first back tube sheet 116 and extends towards the direction away from the first shell 21, first rear cylinder body Inner cavity be formed as the first reaction gas overcurrent chamber 141.The first rear cylinder body 14 and the first rear flange 81 in the present embodiment are one whole Body formula structure.

The second connecting portion includes the second conveyor front barrel 23 and the second forward flange 83 to link together, second conveyor front barrel 23 It is connected on the second front tube sheet 34 and extends towards the direction away from second housing 21, the inner cavity of second conveyor front barrel 23 is formed as Second reaction gas overcurrent chamber 231.The second conveyor front barrel 23 and the second forward flange 83 in the present embodiment are integral formula structure.

First reaction gas overcurrent chamber 141 and the second reaction gas overcurrent chamber 231 are collectively formed as a reaction gas overcurrent chamber.

Using 63 connection of omega sealing between the first rear flange 81 and the second forward flange 83.Both first connecting portion and the It is tightly connected between two interconnecting pieces using omega.

It is appreciated that in other embodiments, first connecting portion can only include the first rear flange 81, only by the second reaction Gas overcurrent chamber 231 forms reaction gas overcurrent chamber.Alternatively, second connecting portion only includes the second forward flange 83, only by the first reaction gas Overcurrent chamber 141 forms reaction gas overcurrent chamber.

The top of second tubular heat exchanger 20 is provided with drum 60, which connects through tedge 613 and down-comer 623 The shell side of the steam generation section 200 of logical second tubular heat exchanger；The top of drum 60 is provided with steam (vapor) outlet 631, which goes out Mouth 631 is connected to the gas returning ports 111 of the first tubular heat exchanger 10 through steam pipe 633.

In the present embodiment, three groups of upper and lower conduits are provided with, every group of upper and lower conduit includes a tedge 613 and one It is lower by pipe 623.First lower port 67 of every tedge 613 is connected to the shell of the second tubular heat exchanger through the top of second housing 21 Journey, the first upper port 65 of tedge 613 is through the inner cavity of the bottom of drum 60 connection drum.

Second lower port 68 of every down-comer 623 is connected to the shell of the second tubular heat exchanger through the obliquely downward of second housing 21 Journey, the inner cavity of the bottom connection drum of the second obliquely downward of the upper port 66 through drum 60 of down-comer.

It is discharged to reduce a large amount of bubbles through steam (vapor) outlet 631, is provided on the inner wall at the top of the shell 61 of drum 60 The underface of steam (vapor) outlet 631 is arranged in one demister 62, the demister 62.

The second tubular heat exchanger of connection is provided on the shell corresponding to the preheating section 300 of the second tubular heat exchanger 20 The water inlet 311 of shell side.

In the present embodiment, the first shell 11 of the first tubular heat exchanger is manufactured using S32168 material, the first tubulation 12 It is made of ALLOY690 material.

First front tube sheet 115 and the first back tube sheet 116 are using 12Cr2mo1 alloy steel casting as substrate, and at this On 12Cr2mo1 alloy steel casting construct Inconel690 alloy welding deposit layer and formed.It is clear to describe, by the first front tube sheet 115 Inconel690 alloy welding deposit layer be known as the first front tube sheet overlay cladding 1151, the Inconel690 alloy of the first back tube sheet 116 Overlay cladding is known as the first back tube sheet overlay cladding 117.Wherein, the first front tube sheet overlay cladding 1151, which is located at, deviates from the first back tube sheet 116 Side, the first back tube sheet overlay cladding 117 be located at away from the first front tube sheet 115 side.

It is with 12Cr2mo1 steel alloy pipe fitting in the first conveyor front barrel 13, reaction gas inlet pipe 132 and the first rear cylinder body 14 For substrate, and constructs on the inner wall of 12Cr2mo1 steel alloy pipe fitting S32168 overlay cladding and formed.In Fig. 2, the first conveyor front barrel 13 and the S32168 overlay cladding label 135 of reaction gas inlet pipe 132 indicate.The S32168 overlay cladding of first rear cylinder body 14 is attached It is not shown in figure.

Second conveyor front barrel 23 is using 12Cr2mo1 steel alloy pipe fitting as substrate, and on the inner wall of 12Cr2mo1 steel alloy pipe fitting Construction S32168 overlay cladding and formed.In the accompanying drawings, the S32168 overlay cladding on the second conveyor front barrel 23 is not shown.

Second front tube sheet 34 is constructed on the 12Cr2mo1 alloy steel casting using 12Cr2mo1 alloy steel casting as substrate Inconel690 alloy welding deposit layer and formed.Label 216 indicates the Inconel690 alloy heap on the second front tube sheet 34 in attached drawing Layer, the Inconel690 alloy welding deposit layer 216 are located at away from the side of the second back tube sheet 35.

Please refer to Fig. 4 and Fig. 5, every second heat exchanger tube 22 includes the first pipeline section 221 and second welded together Pipeline section 222 polishes the welding material for protruding outward outer tube wall to postwelding between first pipeline section 221 and the second pipeline section 222.In In the present embodiment, the first pipeline section 221 is welded on the second front tube sheet, and the second pipeline section 222 is welded on the second back tube sheet.First pipe The length of section is substantially controlled to be preferred in 450-700mm, may further be limited in 500-600mm.In Fig. 4, label 228 is indicated The weld seam of first pipeline section 221 and the second front tube sheet of the second heat exchanger tube 22.In Fig. 5, label 229 indicates the of the second heat exchanger tube 22 Weld seam between one pipeline section 221 and the second pipeline section 222, the weld seam are smoothed.

And the material of first pipeline section is ALLOY690, the material of the second pipeline section is 15CrMo.

In Fig. 1, it is connected on reaction gas inlet pipe 132 in ammonia convertor 900 through synthesis gas outlet 93, makes ammonia convertor 900 inner cavity 91 is connected to the tube side of the first tubular heat exchanger 10.

The process for carrying out ammonia synthesis heat recovering process using above-mentioned integral type ammonia synthesis heat recovery equipment is said below Bright, which is broadly divided into two steps, specifically:

(1) supplement water is entered the shell side of the second tubular heat exchanger by water inlet, is then entered in drum through tedge, Partial moisture evaporates to form saturated vapor, which is entered the shell side of the first tubular heat exchanger by gas returning port, after heat absorption It forms superheated steam and is exported by superheated steam and is discharged, the part water body in drum returns to the second tubular heat exchanger through down-comer Shell side, to the water body continuous heating in drum；

(2) from ammonia convertor 900 be discharged ammonia synthesis gas reaction gas inlet portion is entered by reaction gas inlet pipe, then into Enter successively by the first heat exchanger tube and the second heat exchanger tube, the reaction gas of last reacted gas outlet portion exports discharge, into lower road Process.

Specifically in the present embodiment, the pressure of saturated vapor is about 4.0MPa, and temperature is about 250 DEG C.The pressure of superheated steam Power is 3.8MPa, and temperature is 420 DEG C.

Temperature of the ammonia synthesis gas in reaction gas inlet portion is 445 DEG C, and temperature is reduced to after entering the second heat exchanger 410 DEG C, the discharge temperature in reaction gas outlet is reduced to about 220 DEG C.

The fluctuation range of each technological parameter when according to production, the pressure oscillation of saturated vapor is controlled in ± 0.1MPa model In enclosing.The range of pressure fluctuations of superheated steam also controls within the scope of ± 0.1MPa, and temperature fluctuation range controls in ± 5 DEG C. The pressure of saturated vapor is controlled in 4.0 ± 0.1MPa, the pressure of superheated steam is 3.8 ± 0.1MPa, superheated steam Temperature is 420 ± 10 DEG C.

The fluctuation range of temperature of the ammonia synthesis gas in reaction gas inlet portion is controlled at ± 5 DEG C, is changed entering second The fluctuation range of temperature after hot device is controlled at ± 5 DEG C, is controlled in the fluctuation range of the discharge temperature of reaction gas outlet ± 5 ℃.Temperature control i.e. by ammonia synthesis gas in reaction gas inlet portion is at 445 ± 5 DEG C, the temperature after entering the second heat exchanger At 410 ± 5 DEG C, the discharge temperature in reaction gas outlet is controlled at 220 ± 5 DEG C for control.